The present disclosure relates to systems, methods, and processes for the production of sugars and conversion products from biomass.
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1. A method for producing xylitol by fermentation of a refined hemicellulose sugar stream derived from a lignocellulosic hydrolysate, the method comprising converting xylose in the refined hemicellulose sugar stream to xylitol through fermentation by a microorganism, wherein at least 70% of xylose from the hydrolysate is converted to xylitol, and wherein the refined hemicellulose sugar stream comprises: 50 to 90% xylose weight/weight relative to total dissolved sugars, at least 10% hexoses weight/weight relative to total dissolved sugars, wherein glucose and fructose comprise at least 50% weight/weight of the hexoses, nitrogen in an amount up to 1000 ppm, less than 200 ppm calcium, and furfural in an amount up to 1000 ppm.
13. A method of producing xylitol from a lignocellulosic hydrolysate, comprising:
(i) extracting hemicellulose sugars from the lignocellulosic hydrolysate, thereby obtaining a hemicellulose sugar stream and a lignocellulose remainder stream;
(ii) contacting the hemicellulose sugar stream with an amine extractant to form a mixture;
(iii) separating from the mixture an organic stream comprising the amine extractant and at least one impurity and a refined hemicellulose sugar stream, the refined hemicellulose stream comprising nitrogen and furfural in an amount up to 1000 ppm, less than 200 ppm calcium, 50 to 90% xylose weight/weight relative to total dissolved sugars, and at least 10% hexoses weight/weight relative to total dissolved sugars, wherein glucose and fructose comprise at least 50% weight/weight of the hexoses;
(iv) fermenting the refined hemicellulose sugar stream to produce a fermentation broth comprising xylitol by converting xylose in the refined hemicellulose sugar stream to xylitol; and
(v) recovering xylitol from the fermentation broth, wherein at least 70% of xylose in the lignocellulosic hydrolysate is converted to xylitol.
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This application is a National Stage Entry of PCT/US2016/012384, filed on Jan. 6, 2016, which claims the benefit of U.S. Provisional Application No. 62/100,791, filed on Jan. 7, 2015, and U.S. Provisional Application No. 62/249,801, filed on Nov. 2, 2015, each incorporated herein by reference in its entirety.
Lignocellulosic biomass is an abundant renewable material that has long been recognized as a potential feedstock for producing chemicals, fuels, and materials, including polyol sugar substitutes such as xylitol. Lignocellulosic biomass comprises primarily cellulose, hemicellulose and lignin. Efficient and cost-effective processes to extract, separate and refine sugars from biomass are still a challenge.
Xylitol is a five-carbon sugar alcohol that has favorable properties as a sugar substitute, including low caloric content, good gastrointestinal tolerance, and near insulin-independent metabolism in humans. Traditionally, xylitol is produced by chemical hydrogenation of a monosaccharide mixture containing xylose in the presence of a metal catalyst, such as Raney nickel, necessitating specialized and expensive equipment for the high pressure and temperature requirements of the reaction. The hydrogenation is non-specific and produces polyols of other monosaccharides present in the reaction mixture that are difficult and costly to separate from the desired xylitol product. Trace metal is undesirable and must also be removed from the product. Overall, this expensive and inefficient process produces xylitol in only 40-60% yield. Some basic research has been performed toward the development of bioprocesses for the production of xylitol, but reasonable yields can only be obtained using pure D-xylose as a feedstock.
As such, there is a pressing need for a method of selecting sugar streams suitable for production of xylitol. The present disclosure addresses this need by providing methods, systems, and compositions to produce xylitol from lignocellulosic biomass. Lignocellulosic biomass can be processed and refined to produce hemicellulose sugar streams, and streams suitable for conversion to xylitol selected. This allows for efficient and cost-effective production of xylitol from renewable sources at an industrial scale.
In one aspect, the disclosure provides a method of producing xylitol from a lignocellulose-containing biomass. In one embodiment, the method comprises: (i) fermenting a refined hemicellulose sugar stream to produce a fermentation broth comprising xylitol; and (ii) recovering xylitol from the fermentation broth, wherein the refined hemicellulose sugar stream has been produced by a process comprising: (a) extracting hemicellulose sugars from the biomass, thereby obtaining a hemicellulose sugar stream and a lignocellulose remainder stream; (b) contacting the hemicellulose sugar stream with an amine extractant to form a mixture; and (c) separating from the mixture an organic stream comprising the amine extractant and at least one impurity and the refined hemicellulose sugar stream. Optionally, the biomass is selected from hardwood, wood-pulp, bagasse, sugarcane leaves, birch, eucalyptus, corn cobs, corn stover, coconut hulls, switchgrass, and wheat straw, such as bagasse and sugarcane leaves.
In some examples, the method further comprises reducing ash and soil content of the biomass prior to extracting hemicellulose sugars from the biomass. Optionally, the reducing comprises one or more stages of slurrying, washing, and dewatering the biomass. In some examples, the extracting hemicellulose sugars comprises hot water extraction. Optionally, the hot water extraction further comprises an acid, such as an inorganic acid. In some examples, the acid is present in an amount up to 2% weight/weight. Optionally, the extracting occurs at a temperature of 100 to 200° C.
In some examples, the amine extractant comprises an amine and a diluent. Optionally, the amine comprises at least 20 carbon atoms, such as trilaurylamime. Optionally, the diluent comprises an alcohol, such as hexanol or 2-ethyl-1-hexanol. In some examples, the diluent comprises a C6-12 monoalcohol, kerosene, or a mixture thereof. In some examples, the at least one impurity is selected from ash, acid soluble lignin, furfural, fatty acids, inorganic acids, organic acids, methanol, proteins, amino acids, glycerol, sterols, rosin acid, and waxy materials.
In some examples, the fermentation broth further comprises a microorganism selected from naturally occurring bacteria, recombinant bacteria, naturally occurring yeast, recombinant yeast, and fungi, such as an E. coli strain. Optionally, the fermenting produces, in less than 80 hours, at least 60 grams of the xylitol per liter of the fermentation broth, such as at least 100 grams of the xylitol per liter of the fermentation broth. Optionally, the fermenting produces the xylitol at a rate of at least 1 g/L/h. In some examples, the fermentation broth comprises less than 1 gram of ethanol per liter.
In some examples, at least 70% of xylose in the biomass is converted to xylitol. Optionally, xylose content of the refined hemicellulose sugar stream is at least 80% the xylose content of the hemicellulose sugar stream. In some examples, the fermenting does not comprise xylose purified by crystallization. Optionally, the refined hemicellulose sugar stream comprises at least 50% xylose weight/weight relative to total dissolved sugars, such as between 50 and 90% xylose weight/weight relative to total dissolved sugars.
In one aspect, the disclosure provides a method for producing xylitol by fermentation of a refined hemicellulose sugar stream derived from a lignocellulosic hydrolysate. In one embodiment, the method comprises converting xylose in the refined hemicellulose sugar stream to xylitol through fermentation by a microorganism, wherein the refined hemicellulose sugar stream comprises: 50 to 90% xylose weight/weight relative to total dissolved sugars, less than 200 ppm calcium, and furfural in an amount up to 1000 ppm. In some examples, the microorganism is selected from naturally occurring bacteria, recombinant bacteria, naturally occurring yeast, recombinant yeast, and fungi, such as an E. coli strain. Optionally, the fermentation produces, in less than 80 hours, at least 60 grams of the xylitol per liter of fermentation broth, such as at least 100 grams of the xylitol per liter of fermentation broth. Optionally, the fermentation produces the xylitol at a rate of at least 1 g/L/h. In some examples, the fermentation broth comprises less than 1 gram of ethanol per liter.
In practicing any of the methods described herein, the refined hemicellulose sugar stream may comprise less than 5% oligomers weight/weight relative to total dissolved sugars. Optionally, the refined hemicellulose sugar stream comprises arabinose in an amount up to 12% weight/weight relative to total dissolved sugars, such as between 3 and 12% arabinose weight/weight relative to total dissolved sugars. Optionally, the refined hemicellulose sugar stream comprises at least 10% hexoses weight/weight relative to total dissolved sugars, such as between 10 and 45% hexoses weight/weight relative to total dissolved sugars. Optionally, the hexoses comprise glucose, galactose, mannose, and fructose. In some examples, glucose and fructose comprise at least 50% weight/weight of the hexoses. Optionally, the ratio of xylose to hexoses is between 1.5:1 and 5:1 weight/weight. Optionally, the refined hemicellulose sugar stream comprises disaccharides in an amount up to 8% weight/weight relative to total dissolved sugars. Optionally, the refined hemicellulose sugar stream comprises ash in an amount up to 0.25% weight/weight. Optionally, the refined hemicellulose sugar stream comprises phenolic compounds, wherein the phenolic compounds are present in amounts less than 200 ppm. Optionally, the refined hemicellulose sugar stream comprises furfural in an amount up to 200 ppm. Optionally, the refined hemicellulose sugar stream comprises less than 200 ppm calcium. Optionally, the refined hemicellulose sugar stream comprises nitrogen in an amount up to 1000 ppm.
In one aspect, the disclosure provides a system for producing xylitol from a lignocellulose-containing biomass. In one embodiment, the system comprises: (i) a hemicellulose extraction unit configured to extract and hydrolyze hemicellulose from the biomass to produce a hemicellulose sugar stream and a lignocellulose remainder stream; (ii) a refining unit in fluid communication with the extraction unit, wherein the refining unit is configured to receive the hemicellulose sugar stream and an amine extractant, and wherein the amine extractant removes impurities from the hemicellulose sugar stream to produce a refined hemicellulose sugar stream; (iii) a sensing unit configured to analyze one or more parameters of the refined hemicellulose sugar stream; (iv) a fermentation unit in fluid communication with the refining unit to receive the refined hemicellulose sugar stream, wherein the fermentation unit is configured to contain the refined stream and a microorganism, and wherein the microorganism facilitates production of the xylitol from a monosaccharide in the refined stream to produce a fermentation broth; and (v) a xylitol refining unit, wherein the xylitol refining unit is configured to remove the xylitol from the fermentation broth. In some examples, the system further comprises a wash unit configured to remove ash and soil from the biomass, wherein the hemicellulose extraction unit is in fluid communication with the wash unit.
In some examples, at least 90% of xylose in the refined hemicellulose sugar stream is converted to xylitol in the fermentation unit. Optionally, the xylitol is produced at a rate of at least 1 g/L/h in the fermentation unit. Optionally, the fermentation broth comprises less than 10 g/L ethanol, such as less than 4.5 g/L ethanol, optionally less than 1 g/L ethanol. In some examples, the biomass is selected from bagasse and sugarcane leaves, or a combination thereof. In some examples, the one or more parameters are selected from pH, light absorbance, conductivity, density, xylose concentration, and hexose concentration
In one aspect, the disclosure provides a fermentation feedstock. In one embodiment, the fermentation feedstock comprises: (i) 50 to 90% xylose weight/weight relative to total dissolved sugars; (ii) 10 to 45% hexoses weight/weight relative to total dissolved sugars; (iii) arabinose in an amount up to 12% weight/weight relative to total dissolved sugars; (iv) disaccharides in an amount up to 8% weight/weight relative to total dissolved sugars; (v) furfural in an amount up to 1000 ppm; and (vi) less than 200 ppm calcium. Optionally, the feedstock further comprises (vii) less than 1000 ppm acetic acid; and (viii) less than 1000 ppm formic acid. In some examples, the feedstock further comprises a microorganism. In another embodiment, the fermentation feedstock comprises: (i) 50 to 90% xylose weight/weight relative to total dissolved sugars; (ii) less than 200 ppm calcium; (iii) furfural in an amount up to 1000 ppm; and (iv) a microorganism. Optionally, the feedstock further comprises 10 to 50% hexoses weight/weight relative to total dissolved sugars. Optionally, the feedstock further comprises arabinose in an amount up to 12% weight/weight relative to total dissolved sugars. Optionally, the feedstock further comprises disaccharides in an amount up to 8% weight/weight relative to total dissolved sugars. Optionally, the feedstock further comprises less than 1000 ppm acetic acid. Optionally, the feedstock further comprises less than 1000 ppm formic acid. In some examples, the feedstock further comprises a C6-12 monoalcohol in an amount up to 100 ppm. In some examples, the feedstock further comprises nitrogen in an amount up to 1000 ppm.
In one aspect, the disclosure provides a fermentation broth. In one embodiment, the fermentation broth comprises: (i) at least 60 g/L xylitol; (ii) less than 10 g/L ethanol; (iii) xylose in an amount up to 50 g/L; (iv) hexoses in an amount up to 35 g/L; (v) furfural in an amount up to 1000 ppm; and (vi) less than 200 ppm calcium. In some examples, the broth further comprises: (vii) less than 1000 ppm acetic acid; and (viii) less than 1000 ppm formic acid. Optionally, the broth further comprises a C6-12 monoalcohol in an amount up to 100 ppm. In some examples, the broth further comprises a microorganism.
In one aspect, the disclosure provides a xylitol composition. In one embodiment, the xylitol composition comprises: (i) at least 98% xylitol weight/weight relative to total dissolved solids; (ii) oligosaccharides in an amount up to 1% weight/weight relative to total dissolved solids; and (iii) hexoses in an amount up to 1%. In some examples, the xylitol composition further comprises ash in an amount up to 0.25% weight/weight relative to total dissolved solids. Optionally, the xylitol composition further comprises furfural in an amount up to 1000 ppm. Optionally, the xylitol composition further comprises an amine in an amount up to 100 ppm, and wherein the amine comprises at least 12 carbon atoms. Optionally, the xylitol composition further comprises a C6-12 monoalcohol in an amount up to 100 ppm. In some examples, the hexoses are selected from glucose, galactose, mannose, and fructose. Optionally, the xylitol composition further comprises less than 100 ppm arabitol, such as less than 1 ppm arabitol. Optionally, the xylitol composition further comprises less than 100 ppm galactitol, such as less than 1 ppm galactitol. Optionally, the composition is derived from a hydrolyzate of a lignocellulose-containing biomass. Optionally, the composition is crystalline. Optionally, the composition is provided as an aqueous solution. In some examples, the aqueous solution comprises at least 50% weight/weight dissolved solids.
In one aspect, the disclosure provides a method of producing a refined hemicellulose sugar stream suitable for conversion to xylitol. In one embodiment, the method comprises: (i) extracting hemicellulose sugars from the biomass, thereby obtaining a hemicellulose sugar stream and a lignocellulose remainder stream; (ii) contacting the hemicellulose sugar stream with an amine extractant to form a mixture; (iii) separating from the mixture an organic stream comprising the amine extractant and at least one impurity and a refined hemicellulose sugar stream; and (iv) measuring concentrations of at least one of xylose, arabinose, hexoses, disaccharides, ash, acetic acid, formic acid, phenolic compounds, furfural, calcium, and nitrogen; wherein the refined hemicellulose sugar stream is suitable for conversion to xylitol if the refined stream comprises: (1) at least 50% xylose weight/weight relative to total dissolved sugars; (2) at least 10% hexoses weight/weight relative to total dissolved sugars; and (3) less than 200 ppm calcium; and wherein the refined stream suitable for conversion to xylitol further comprises at least one characteristic selected from: (4) arabinose in an amount up to 12% weight/weight relative to total dissolved sugars; (5) disaccharides in an amount up to 8% weight/weight relative to total dissolved sugars; (6) ash in an amount up to 0.25% weight/weight; (7) less than 1000 ppm acetic acid; (8) less than 1000 ppm formic acid; (9) phenolic compounds in an amount up to 200 ppm; (10) furfural in an amount up to 200 ppm; and (11) nitrogen in an amount up to 1000 ppm; and wherein a refined stream unsuitable for conversion to xylitol is further refined.
In some examples, the refined stream suitable for conversion to xylitol further comprises furfural in an amount up to 200 ppm. Optionally, the refined stream suitable for conversion to xylitol further comprises arabinose in an amount up to 12% weight/weight relative to total dissolved sugars. Optionally, the refined stream suitable for conversion to xylitol further comprises disaccharides in an amount up to 8% weight/weight relative to total dissolved sugars. Optionally, the refined stream suitable for conversion to xylitol further comprises ash in an amount up to 0.25% weight/weight. Optionally, the refined stream suitable for conversion to xylitol further comprises acetic acid in an amount up to 1000 ppm. Optionally, the refined stream suitable for conversion to xylitol further comprises formic acid in an amount up to 1000 ppm. Optionally, the refined stream suitable for conversion to xylitol further comprises phenolic compounds in an amount up to 200 ppm. Optionally, the refined stream suitable for conversion to xylitol further comprises nitrogen in an amount up to 1000 ppm.
All publications, patents, and patent applications mentioned in this specification are herein incorporated by reference to the same extent as if each individual publication, patent, or patent application was specifically and individually indicated to be incorporated by reference. PCT/IL2012/050118 filed Apr. 2, 2012, PCT/US2013/039585 filed May 3, 2013, PCT/US2013/068824 filed Nov. 6, 2013, PCT/US2014/053956 filed Sep. 3, 2014, U.S. App. No. 62/100,791 filed Jan. 7, 2015, and U.S. App. No. 62/249,801 filed Nov. 2, 2015 are incorporated by reference.
The present disclosure relates to lignocellulosic biomass processing and refining to produce hemicellulose sugars, and the conversion thereof to high-value products (e.g., xylitol). Conversion of the hemicellulose sugars to high-value products may be completed by any suitable chemical, catalytic, enzymatic, metabolic, fermentation, or bioconversion process, or a combination thereof. Optionally, hemicellulose sugars are converted to high-value products by a fermentation process.
In one aspect, the disclosure provides a method of producing xylitol from a lignocellulose-containing biomass. In one example, the method comprises: (i) extracting hemicellulose sugars from the biomass, thereby obtaining a hemicellulose sugar stream and a lignocellulose remainder stream; (ii) contacting the hemicellulose sugar stream with an extractant (e.g., an amine extractant) to form a mixture; and (iii) separating from the mixture an organic stream comprising the extractant and at least one impurity and a refined hemicellulose sugar stream. Optionally, the method further comprises: (iv) fermenting the refined hemicellulose sugar stream to produce a fermentation broth comprising xylitol; and (v) recovering xylitol from the fermentation broth. Optionally, the method further comprises reducing ash and soil content of the biomass prior to extracting hemicellulose sugars from the biomass.
In one aspect, the disclosure provides a method of producing xylitol by fermentation of a refined hemicellulose sugar stream derived from a lignocellulosic hydrolysate. In one example, the method comprises converting xylose in the refined hemicellulose sugar stream to xylitol through fermentation by a microorganism. Optionally, the hemicellulose sugar stream comprises: 50 to 90% xylose weight/weight relative to total dissolved sugars, less than 200 ppm calcium, and furfural in an amount up to 1000 ppm.
In one aspect, the disclosure provides a method of producing a refined hemicellulose sugar stream suitable for conversion to xylitol. In one example, the method comprises: (i) extracting hemicellulose sugars from the biomass, thereby obtaining a hemicellulose sugar stream and a lignocellulose remainder stream; (ii) contacting the hemicellulose sugar stream with an extractant (e.g., an amine extractant) to form a mixture; (iii) separating from the mixture an organic stream comprising the extractant and at least one impurity and a refined hemicellulose sugar stream; and (iv) measuring concentrations of at least one of xylose, arabinose, hexoses, disaccharides, ash, acetic acid, formic acid, phenolic compounds, furfural, levulinic acid, calcium, and nitrogen; wherein a refined hemicellulose sugar stream is suitable for conversion to xylitol if the refined stream comprises: (1) at least 50% xylose weight/weight relative to total dissolved sugars; (2) at least 10% hexoses weight/weight relative to total dissolved sugars; and (3) less than 200 ppm calcium; and wherein the refined stream suitable for conversion to xylitol further comprises at least one characteristic selected from: (4) arabinose in an amount up to 12% weight/weight relative to total dissolved sugars; (5) disaccharides in an amount up to 8% weight/weight relative to total dissolved sugars; (6) ash in an amount up to 0.25% weight/weight; (7) acetic acid in amount up to 1000 ppm; (8) formic acid in amount up to 1000 ppm; (9) phenolic compounds in an amount up to 200 ppm; (10) furfural in an amount up to 200 ppm; and (11) nitrogen in an amount up to 1000 ppm; and wherein a refined stream unsuitable for conversion to xylitol is further refined.
A biomass embodied in a subject method or system disclosed herein is typically high in xylan content. The biomass may be derived from wood, softwood, hardwood such as alder, aspen, birch, beech, maple, poplar, eucalyptus, and willow, plants or plant constituents, grains such as wheat, barley, rice, rye and oat, particulates of grain such as straw, hulls, husks, fiber, shells, and stems, corn cobs, corn straw, corn fiber, nutshells, almond shells, coconut shells, bagasse, cottonseed bran, and cottonseed skins. When wood is used as a starting material, it is advantageously used as chips or sawdust. Preferably, the biomass is selected from hardwood, such as birch and eucalyptus, bagasse, and sugarcane leaves, or a combination thereof.
A schematic of exemplary conversion processes to convert biomass to a refined hemicellulose sugar stream is provided in
Pretreatment of the lignocellulose-containing biomass may comprise reducing ash and soil content of the biomass prior to extracting hemicellulose sugars from the biomass. In some examples, lignocellulose-containing biomass comprising greater than about 4% wt/wt, greater than about 5% wt/wt, greater than about 6% wt/wt, greater than about 7% wt/wt, or greater than about 8% wt/wt apparent ash (as measured by ashing a dry sample of the biomass according to NREL/TP-510-42622) is de-soiled and de-ashed. Ash values greater than about 4% may be indicative of physical incorporation of soil particles in the biomass during the growing season, wherein the soil particles contact and are encased by the biomass as it grows. Reducing ash and soil content of the biomass may comprise one or more stages of slurrying, washing, and dewatering the biomass. A method for reducing ash and soil content may comprise at least one and up to n stages of re-slurry and milling (e.g., grinding) the biomass, and at least one and up to m stages of washing and dewatering the biomass, wherein n is 2, 3, 4, 5, 6, 7, 8, 9 or 10 and m is 2, 3, 4, 5, 6, 7, 8, 9 or 10. Optionally, n is equal to m. In some examples, m is greater than n or n is greater than m. Two or more such cycles of shear treatment and high pressure washing may be necessary to reduce the ash content of the biomass to less than 6%, less than 5%, less than 4%, or less than 3% wt/wt ash.
Hemicellulose sugars may be extracted from lignocellulosic biomass by any suitable method (1700), for example, using an aqueous acidic solution. The aqueous acidic solution may comprise any acid, such as an inorganic acid or an organic acid. Preferably, the solution comprises an inorganic acid, such as H2SO4, H2SO3 (which can be introduced as dissolved acid or as SO2 gas), or HCl. In some examples, the aqueous acidic solution may comprise an inorganic and/or an organic acid, including, for example, H2SO4, H2SO3, HCl, or acetic acid, or combinations thereof. The acidic aqueous solution can contain an acid in an amount of about 0 to 2% acid or more, such as about 0-1.0%, about 0-1.5%, about 0.5-1.5%, about 0.5-2.0%, about 1.0-2.0%, about 1.5-2.0%, about 0.2-1.0%, about 0.2-0.7%, about 0-0.2%, about 0.2-0.4%, about 0.4-0.6%, about 0.6-0.8%, about 0.8-1.0%, about 1.0-1.2%, about 1.2-1.4%, about 1.4-1.6%, about 1.6-1.8%, or about 1.8-2.0% wt/wt. Optionally, the aqueous solution for the extraction includes 0.2-0.7% H2SO4 and 0-3,000 ppm SO2. The pH of the acidic aqueous solution may be in the range of about pH 1 to pH 5, such as about pH 1 to pH 3.5.
Elevated temperature or pressure may be used to extract hemicellulose sugars from biomass. In some examples, a temperature in the range of about 100-200° C. is used. A temperature of greater than 50° C., greater than 60° C., greater than 70° C., greater than 80° C., greater than 90° C., greater than 100° C., greater than 110° C., greater than 120° C., greater than 130° C., greater than 140° C., greater than 150° C., greater than 160° C., greater than 170° C., greater than 180° C., greater than 190° C., or greater than 200° C. can be used in the extraction. Preferably, the temperature is in the range of 90-170° C., such as 100-165° C., 110-160° C., 120-150° C., 130-155° C. or 140-150° C. The pressure can be in the range of about 0.4-10 mPa, such as 0.4-5 mPa. Optionally, the pressure is less than 20 mPa, such as less than 10 mPa, less than 9 mPa, less than 8 mPa, less than 7 mPa, less than 6 mPa, or less than 5 mPa. In some examples, the extraction mixture is heated for 0.1-5 hours, preferably 0.1-3 hours, 0.1-1 hour, 0.5-1.5 hours, 0.5-2 hours, 1-2 hours, or 2-3 hours. The extraction process can have a cooling down period of less than one hour. Optionally, hemicellulose sugars are extracted from biomass by contacting the biomass with an aqueous acidic solution and heating the resultant mixture to a temperature of greater than 50° C. at a pressure of less than 10 mPa.
Hemicellulose sugar extraction can produce, in one single extraction process, a hemicellulose sugar stream (1700-A) containing at least 75% monomeric sugars, such as more than 80%, more than 85%, more than 90%, more than 91%, more than 92%, more than 93%, more than 94%, more than 95%, more than 96%, more than 97%, more than 98%, or more than 99% monomeric sugars. The hemicellulose sugar stream may contain 80-99% monomeric sugars. In some examples, at least about 70%, at least 75%, at least 80%, at least 85%, at least 90%, or even at least 95% or more of the hemicellulose sugars present in the biomass can be extracted using a method of the disclosure. Hemicellulose sugar extraction may produce minimal amounts of lignocellulose degradation products, such as furfural, hydroxymethyl furfural, levulinic acid, and formic acid. A xylose yield of greater than 70%, optionally greater than 80%, of theoretical value can be achieved.
The extraction of hemicellulose sugars from the biomass results in a lignocellulose remainder stream (1700-P1) comprising lignin and cellulose. A schematic diagram of exemplary sequential processes for washing and de-watering a lignocellulose remainder stream after extraction of hemicellulose sugars is provided in
Impurities such as ash, acid soluble lignin, furfural, fatty acids, organic acids such as acetic acid and formic acid, methanol, proteins and/or amino acids, glycerol, sterols, rosin acid or waxy materials, or combinations thereof, can be extracted together with the hemicellulose sugars under the same conditions into the hemicellulose sugar stream. At least some of these impurities can be separated from the hemicellulose sugar stream by solvent extraction (e.g., using an amine extractant).
The hemicellulose sugar stream can be refined and optionally fractionated according to processes disclosed in PCT/US2013/039585, incorporated herein by reference. The hemicellulose sugar stream can be optionally filtered, centrifuged, or concentrated by evaporation. Optionally, the hemicellulose sugar stream is contacted with a strong acid cation exchanger (e.g., in H+ form) to convert salts to the respective acids. In some examples, the hemicellulose sugar stream is first contacted with a strong cation exchange resin and then contacted with an amine extractant.
Optionally, impurities are removed from the hemicellulose sugar stream by contacting the stream with an amine extractant to form a mixture, wherein the mixture may comprise an organic stream and an aqueous stream (1710). Exemplary conversion processes for the purification of the hemicellulose sugar stream (1700-A and 1800-A) are depicted in
The amine extractant may comprise 10-90%, such as 10-80%, 10-70%, 10-60%, 10-50%, 10-40%, 20-80%, 20-70%, 20-60%, 20-50%, 20-40%, 15-80%, 15-70%, 15-60%, 15-50%, 15-40%, 15-35%, 25-80%, 25-70%, 25-60%, 25-50%, 25-40%, or 25-35% weight/weight of one or more amines having at least 20 carbon atoms. Such amine(s) can be primary, secondary, or tertiary amines. Examples of tertiary amines include trilaurylamine (TLA; e.g. COGNIS ALAMINE 304 from Cognis Corporation; Tucson Ariz.; USA), trioctylamine, tri-isooctylamine, tri-caprylylamine and tri-decylamine.
The amine extractant may further comprise a diluent. In some examples, the amine extractant comprises at least 10%, at least 20%, at least 30%, at least 40%, at least 50%, at least 60%, at least 70%, at least 80%, or at least 90% weight/weight, such as 55-85% weight/weight, of a diluent. Optionally, the diluent is an alcohol, such as butanol, isobutanol, pentanol, hexanol, octanol, decanol, dodecanol, tetradecanol, pentadecanol, hexadecanol, octadecanol, eicosanol, docosanol, tetracosanol, and triacontanol. Optionally, the diluent is a long chain alcohol (e.g. C6, C8, C10, C12, C14, C16 alcohol), or kerosene. In some examples, the diluent is n-hexanol or 2-ethyl-1-hexanol. Optionally, the diluent is 2-ethyl-1-hexanol. In some examples, the diluent comprises one or more additional components, such as a ketone, an aldehyde having at least 5 carbon atoms, or another alcohol.
Optionally, the amine extractant comprises an amine having at least 20 carbon atoms and a diluent (e.g., an alcohol), such as a tertiary amine having at least 20 carbon atoms and an alcohol. In some examples, the amine extractant comprises a tertiary amine having from 20 to 50 carbon atoms and a diluent, wherein the diluent is a C6-12 monoalcohol. In some examples, the amine extractant comprises an amine having from 24-40 carbon atoms (e.g., trilaurylamine, trioctylamine, tricaprylylamine, or tridecylamine) and a diluent, wherein the diluent is a C6-12 monoalcohol (e.g., hexanol, octanol, or 2-ethylhexanol). In some examples, the amine is trilaurylamine and the diluent is hexanol or 2-ethylhexanol.
The amine extractant can comprise an amine and a diluent in a ratio between 1:10 and 10:1 weight/weight, such as 1:9, 1:4, 3:7, 2:3, 1:1, 3:2, 7:3, 4:1, or 9:1 weight/weight. Optionally, the amine extractant comprises trilaurylamine and a C6-12 monoalcohol in a ratio of 1:7, 2:7, 3:7, 6:4, 5.5:4.55, 4:7, 5:7, 6:7, 7:7, 5:4, 3:4, 2:4, or 1:4 weight/weight. Optionally, the amine extractant comprises trilaurylamine and a C6-12 monoalcohol in a ratio of about 3:7 weight/weight, such as a 3:7 weight/weight ratio of trilaurylamine and hexanol.
Optionally, the hemicellulose sugar stream is extracted with an amine extractant counter-currently, e.g., the hemicellulose sugar stream flows in a direction opposite to the flow of the amine extractant. The amine extraction can be conducted at any temperature at which the amine is soluble, such as 50-70° C. Optionally, the amine extraction comprises more than one extraction step (e.g., 2, 3, or 4 steps). The ratio of the amine extractant stream (organic stream) to the hemicellulose sugar stream (aqueous stream) can range from about 0.5:1 to about 5:1 weight/weight, such as about 0.5:1, about 1:1, about 1.5:1, about 2:1, about 2.5:1, about 3:1, about 3.5:1, about 4:1, about 4.5:1, or about 5:1. In some examples, the ratio of the organic stream to the aqueous stream is about 1.5-3.0:1 weight/weight.
After contacting the hemicellulose sugar stream with the amine extractant, the resulting mixture can be separated into an organic stream (i.e., the organic phase) comprising the amine extractant and at least one impurity and a refined hemicellulose sugar stream (i.e., the aqueous phase). At least a portion of organic acids or inorganic acids (e.g., the acids used in hemicellulose sugar extraction) and other impurities may be extracted into the organic stream. In some examples, the organic stream is contacted with an aqueous stream in a counter current mode to recover any residual sugars absorbed into the organic stream. The organic stream may comprise less than 5%, less than 4%, less than 3%, less than 2%, less than 1%, less than 0.8%, less than 0.6%, less than 0.5%, less than 0.4%, less than 0.3%, less than 0.2%, or less than 0.1% weight/weight hemicellulose sugars, such as 0.01% to 4% hemicellulose sugars. In some examples, the refined hemicellulose sugar stream comprises less than 3%, less than 2%, less than 1%, less than 0.8%, less than 0.6%, less than 0.5%, less than 0.4%, less than 0.3%, less than 0.2%, or less than 0.1% weight/weight acid, such as 0.01% to 3% acid. In some examples, the refined hemicellulose sugar stream comprises less than 5%, less than 4%, less than 3%, less than 2%, less than 1%, less than 0.8%, less than 0.6%, less than 0.5%, less than 0.4%, less than 0.3%, less than 0.2%, or less than 0.1% weight/weight of an amine having at least 20 carbon atoms, such as 0.01% to 4% of an amine. In some examples, the refined hemicellulose sugar stream comprises less than 5%, less than 4%, less than 3%, less than 2%, less than 1%, less than 0.8%, less than 0.6%, less than 0.5%, less than 0.4%, less than 0.3%, less than 0.2%, or less than 0.1% weight/weight of an impurity, such as 0.1% to 4% of an impurity, wherein the impurity is selected from ash, acid soluble lignin, furfural, fatty acids, organic acids such as acetic acid and formic acid, mineral acids such as hydrochloric acid and sulfuric acid, furfural, hydroxymethylfurfural, methanol, proteins, amino acids, glycerol, sterols, rosin acid, and waxy materials. The refined hemicellulose sugar stream may comprise less than 5%, less than 4%, less than 3%, less than 2%, less than 1%, less than 0.8%, less than 0.6%, less than 0.5%, less than 0.4%, less than 0.3%, less than 0.2%, or less than 0.1% weight/weight furfural, such as 0.1% to 4% of furfural. In some examples, the refined hemicellulose sugar stream comprises less than 5%, less than 4%, less than 3%, less than 2%, less than 1%, less than 0.8%, less than 0.6%, less than 0.5%, less than 0.4%, less than 0.3%, less than 0.2%, or less than 0.1% weight/weight ash, such as 0.1% to 4% of ash.
The refined hemicellulose sugar stream can be further purified. For example, residual diluent in the refined hemicellulose sugar stream can be removed using a packed distillation column. The distillation can remove at least 70%, at least 80%, at least 90%, or at least 95% of residual diluent in the refined hemicellulose sugar stream. In some examples, the refined hemicellulose sugar stream is contacted with a strong acid cation (SAC) exchanger (1833) to remove residual metallic cations and residual amines, then optionally contacted with a weak base anion (WBA) exchanger (1834) to remove excess protons. Optionally, the refined hemicellulose sugar stream is purified using a distillation column (e.g., a packed distillation column) followed by a strong acid cation exchanger. In some examples, the refined hemicellulose sugar stream is contacted with a weak base anion (WBA) exchanger to remove excess protons. The refined hemicellulose sugar stream can be pH adjusted, optionally after contacting the stream with a SAC exchanger and/or WBA exchanger. The refined hemicellulose sugar stream can be distilled or evaporated, then further polished by contacting with a SAC resin, a WBA resin, and a MB resin, and optionally concentrated by evaporation. In some examples, the refined hemicellulose sugar stream is evaporated (1835) to 20-80% weight/weight dissolved sugars, such as 25-65% or 30-40% weight/weight dissolved sugars, thereby forming a concentrated sugar solution (1836). The evaporation may be conducted in any conventional evaporator, e.g., a multiple effect evaporator or a mechanical vapor recompression (MVR) evaporator.
Residual solvent present in the hemicellulose sugar stream or concentrated sugar solution can also be removed by evaporation. For example, a solvent that forms a heterogeneous azeotrope with water can be separated and optionally returned to the solvent cycle. Optionally, the refined hemicellulose sugar stream can be contacted with activated carbon to remove residual organic impurities. The refined hemicellulose sugar stream may also be contacted with mixed bed resin system to remove any residual ions or color bodies.
The refined hemicellulose sugar stream produced by the subject systems and methods can comprise sugars in a ratio highly suitable as feed for fermentation, such as for the production of xylitol.
In some examples, the refined hemicellulose sugar stream comprises at least 40%, at least 45%, at least 50%, at least 55%, at least 60%, at least 65%, at least 70%, at least 75%, at least 80%, at least 85%, at least 90%, or at least 95% weight/weight xylose relative to total dissolved sugars. Optionally, the refined hemicellulose sugar stream comprises between 40% and 95% weight/weight xylose relative to total dissolved sugars, such as 50% to 85% xylose.
In some examples, the refined hemicellulose sugar stream comprises less than 15%, less than 14%, less than 13%, less than 12%, less than 11%, less than 10%, less than 9%, less than 8%, less than 7%, less than 6%, less than 5%, less than 4%, less than 3%, or less than 2% weight/weight arabinose relative to total dissolved sugars. Optionally, the refined hemicellulose sugar stream comprises between 1% and 15% weight/weight arabinose relative to total dissolved sugars, such as 3% to 12% arabinose.
In some examples, the refined hemicellulose sugar stream comprises at least 5%, at least 10%, at least 12%, at least 15%, at least 17%, at least 20%, at least 22%, at least 25%, at least 27%, at least 30%, at least 32%, at least 35%, at least 37%, at least 40%, at least 42%, at least 45%, at least 50%, at least 52%, at least 55%, or at least 57% weight/weight hexoses relative to total dissolved sugars. Optionally, the refined hemicellulose sugar stream comprises between 5% and 60% weight/weight hexoses relative to total dissolved sugars, such as 10% to 45% hexoses.
In some examples, the hexoses comprise glucose, galactose, mannose and fructose, wherein glucose and fructose optionally comprise at least 30%, at least 40%, at least 45%, at least 50%, at least 55%, at least 60%, at least 65%, at least 70%, at least 75%, or at least 80% weight/weight of the hexoses. Optionally, the refined hemicellulose sugar stream comprises between 30% and 85% weight/weight glucose and fructose relative to hexoses, such as 50% to 80% glucose and fructose.
In some examples, the refined hemicellulose sugar stream comprises at least 5%, at least 10%, at least 12%, at least 15%, at least 17%, at least 20%, at least 22%, at least 25%, at least 27%, at least 30%, at least 32%, at least 35%, at least 37%, at least 40%, at least 42%, at least 45%, at least 50%, at least 52%, at least 55%, or at least 57% weight/weight glucose relative to total dissolved sugars. Optionally, the refined hemicellulose sugar stream comprises between 5% and 60% weight/weight glucose relative to total dissolved sugars, such as 10% to 45% glucose.
In some examples, the refined hemicellulose sugar stream comprises xylose in a ratio to hexoses of at least 1:1 weight/weight, such as at least 1.5:1, at least 2:1, at least 3:1, at least 4:1, at least 5:1, at least 6:1, or at least 7:1 weight/weight. Optionally, the ratio of xylose to hexoses in the refined hemicellulose sugar stream is between 1:1 and 8:1 weight/weight, such as between 1.5:1 and 5:1 weight/weight.
In some examples, the refined hemicellulose sugar stream comprises less than 15%, less than 10%, less than 9%, less than 8%, less than 7%, less than 6%, less than 5%, less than 4%, less than 3%, less than 2%, or less than 1% weight/weight disaccharides relative to total dissolved sugars. Optionally, the refined hemicellulose sugar stream comprises between 0.1% and 15% weight/weight disaccharides relative to total dissolved sugars, such as 0.5% to 8% disaccharides.
In some examples, the refined hemicellulose sugar stream comprises less than 16%, less than 14%, less than 12%, less than 10%, less than 8%, less than 6%, less than 5%, less than 4%, less than 3%, less than 2%, less than 1%, or less than 0.5% weight/weight oligosaccharides relative to total dissolved sugars, wherein said oligosaccharides comprise at least 3 monosaccharide units. Optionally, the refined hemicellulose sugar stream comprises between 0.1% and 10% weight/weight oligosaccharides relative to total dissolved sugars, such as 0.5% to 5% oligosaccharides.
In some examples, the refined hemicellulose sugar stream comprises ash in an amount up to 2%, up to 1.5%, up to 1%, up to 0.75%, up to 0.50%, up to 0.25%, up to 0.1%, or up to 0.05% weight/weight ash. Optionally, the refined hemicellulose sugar stream comprises between 0.001% and 1% weight/weight ash, such as 0.001% to 0.25% ash.
In some examples, the ash comprises Ca, Cu, Fe, K, Mg, Mn, Na, P, S, or Si, or a combination thereof. In some examples, the refined hemicellulose sugar stream comprises Ca, Cu, Fe, K, Mg, Mn, Na, P, S, and Si at less than 1000 ppm, less than 750 ppm, less than 500 ppm, less than 400 ppm, less than 300 ppm, less than 200 ppm, less than 100 ppm, less than 50 ppm, or less than 10 ppm each. Optionally, the refined hemicellulose sugar stream comprises between 1 ppm and 1000 ppm each of Ca, Cu, Fe, K, Mg, Mn, Na, P, S, and Si, such as 1 ppm to 250 ppm each of Ca, Cu, Fe, K, Mg, Mn, Na, P, S, and Si. In some examples, the refined hemicellulose sugar stream comprises less than 1000 ppm, less than 750 ppm, less than 500 ppm, less than 400 ppm, less than 300 ppm, less than 200 ppm, less than 100 ppm, less than 50 ppm, or less than 10 ppm calcium. Optionally, the refined hemicellulose sugar stream comprises between 1 ppm and 1000 ppm of calcium, such as 1 ppm to 250 ppm calcium.
In some examples, the refined hemicellulose sugar stream comprises phenolic compounds in amounts up to 1000 ppm, up to 750 ppm, up to 500 ppm, up to 400 ppm, up to 300 ppm, up to 200 ppm, up to 100 ppm, up to 50 ppm, or up to 10 ppm. Optionally, the refined hemicellulose sugar stream comprises between 1 ppm and 1000 ppm phenolic compounds, such as 1 ppm to 250 ppm phenolic compounds.
In some examples, the refined hemicellulose sugar stream comprises furfural in an amount up to 1000 ppm, up to 750 ppm, up to 500 ppm, up to 400 ppm, up to 300 ppm, up to 200 ppm, up to 100 ppm, up to 50 ppm, or up to 10 ppm. Optionally, the refined hemicellulose sugar stream comprises between 1 ppm and 1000 ppm of furfural, such as 1 ppm to 250 ppm furfural.
In some examples, the refined hemicellulose sugar stream comprises less than 1000 ppm, less than 750 ppm, less than 500 ppm, less than 400 ppm, less than 300 ppm, less than 200 ppm, less than 100 ppm, less than 50 ppm, or less than 10 ppm organic acids, such as acetic acid, levulinic acid, formic acid, and lactic acid. Optionally, the refined hemicellulose sugar stream comprises between 1 ppm and 1000 ppm organic acids, such as 1 ppm to 250 ppm organic acids. Optionally, the refined hemicellulose sugar stream comprises between 1 ppm and 1000 ppm of acetic acid, such as 1 ppm to 250 ppm acetic acid. Optionally, the refined hemicellulose sugar stream comprises between 1 ppm and 1000 ppm of formic acid, such as 1 ppm to 250 ppm formic acid.
In some examples, the refined hemicellulose sugar stream comprises an amine in an amount up to 1000 ppm, up to 750 ppm, up to 500 ppm, up to 400 ppm, up to 300 ppm, up to 200 ppm, up to 100 ppm, up to 50 ppm, or up to 10 ppm, and wherein the amine comprises at least 12 carbon atoms. Optionally, the amine is a laurylamine, such as monolaurylamine, dilaurylamine, or trilaurylamine. Optionally, the refined hemicellulose sugar stream comprises between 0.1 ppm and 1000 ppm of an amine comprising at least 12 carbon atoms, such as 0.1 ppm to 250 ppm of an amine comprising at least 12 carbon atoms.
In some examples, the refined hemicellulose sugar stream comprises an alcohol in an amount up to 1000 ppm, up to 750 ppm, up to 500 ppm, up to 400 ppm, up to 300 ppm, up to 200 ppm, up to 100 ppm, up to 50 ppm, or up to 10 ppm. The alcohol can be any alcohol that can be used herein as a diluent, such as butanol, pentanol, hexanol, or 2-ethyl-1-hexanol. In some examples, the alcohol is a C6-12 monoalcohol, optionally present in the refined hemicellulose sugar stream in an amount up to 200 ppm. Optionally, the refined hemicellulose sugar stream comprises between 1 ppm and 1000 ppm of said alcohol, such as 1 ppm to 250 ppm of said alcohol.
In some examples, the refined hemicellulose sugar stream comprises nitrogen in an amount up to 1000 ppm, up to 750 ppm, up to 500 ppm, up to 400 ppm, up to 300 ppm, up to 200 ppm, or up to 150 ppm. Optionally, the refined hemicellulose sugar stream comprises between 1 ppm and 1000 ppm of nitrogen, such as 1 ppm to 250 ppm nitrogen. Nitrogen may be total Kjeldahl nitrogen measured using the Kjeldahl method.
In some examples, the refined hemicellulose sugar stream comprises: at least 50% weight/weight xylose; arabinose in an amount up to 12% weight/weight; at least 10% weight/weight hexoses; disaccharides in an amount up to 8% weight/weight; ash in an amount up to 0.25% weight/weight; furfural in an amount up to 200 ppm; and nitrogen in an amount up to 1000 ppm. In some examples, the refined hemicellulose sugar stream comprises: at least 50% weight/weight xylose; between 3% and 12% weight/weight arabinose; at least 10% weight/weight hexoses; between 0.001% and 0.25% weight/weight ash; between 1 ppm and 200 ppm furfural; and between 1 ppm and 1000 ppm nitrogen. Optionally, the refined hemicellulose sugar stream comprises 65-75% xylose, 3-10% arabinose and 15-25% hexoses (all weight/weight relative to total dissolved sugars). The refined hemicellulose sugar stream can contain at least 90% weight/weight saccharides relative to total dissolved solids, such as at least 91%, at least 92%, at least 93%, at least 94%, at least 95%, at least 96%, at least 97%, at least 98%, at least 99%, or at least 99.5% saccharides.
The refined hemicellulose sugar stream can have a high purity with respect to ash elements, organic acids, lignin derivatives and sugar degradation products. The refined hemicellulose sugar stream may comprise ash at a concentration of up to 1%, up to 0.5%, up to 0.1%, up to 0.05%, or up to 0.01% weight/weight relative to total dissolved sugars, wherein the ash comprises up to 500 ppm, up to 250 ppm, or up to 100 ppm metallic cations and less than 100 ppm, less than 50 ppm, less than 30 ppm, or less than 20 ppm sulfur relative to total dissolved sugars. In some examples, a refined hemicellulose sugar stream is particularly suitable for fermentation processes that are sensitive to ash elements or to sulfur compounds. The refined hemicellulose sugar stream can comprise less than 5000 ppm ash in total weight/weight relative to xylose, wherein the ash comprises elements selected from Na, Ca, Cu, Fe, K, Mg, Mn, S and P.
In some examples, the refined hemicellulose sugar stream comprises at least one characteristic selected from: (i) a ratio of disaccharides to total dissolved sugars of not more than 0.10 weight/weight; (ii) a ratio of xylose to total dissolved sugars of at least 0.70 weight/weight; (iii) a ratio of arabinose to total dissolved sugars of not more than 0.06 weight/weight; (iv) a ratio of galactose to total dissolved sugars of not more than 0.05 weight/weight; (v) a ratio of the sum of the glucose and fructose to total dissolved sugars of not more than 0.15 weight/weight; (vi) a ratio of mannose to total dissolved sugars of not more than 0.05 weight/weight; (vii) a ratio of fructose to total dissolved sugars of not more than 0.10 weight/weight; (viii) phenolic compounds in an amount of not more than 1000 ppm; (ix) hexanol in an amount of not more than 0.1% weight/weight: (x) furfural in an amount of not more than 1000 ppm; (xi) organic acids in an amount of not more than 1000 ppm; and (xii) less than 1000 ppm each of the elements Ca, Cu, Fe, K, Mg, Mn, S and P relative to total dissolved sugars.
In some examples, the refined hemicellulose sugar stream comprises low levels of additional monosaccharides and disaccharides. Optionally, the additional monosaccharides are selected from lyxose, xylulose, and ribulose. Optionally, the additional disaccharides are selected from gentiobiose, sophorose, nigerose, laminaribiose, and kojibiose. These additional monosaccharides and disaccharides may be beneficial to fermentation processes. In some examples, such rare saccharides are biologically active and may act as promoters to increase activity of enzymatic expression or work as cofactors to increase activity of the enzymes, thus resulting in accelerated biological conversion.
Surprisingly, the refined hemicellulose sugar stream is particularly advantageous in a fermentation process capable of hydrogenating xylose to xylitol, as the fermenting species can utilize the hexoses as their energy source, thus, in some examples, eliminating the need to further purify or fractionate the sugar stream prior to the hydrogenation step. Further purification steps commonly used to enrich the xylose content of a sugar stream, such as chromatographic separation or crystallization, may not be necessary before fermentation. In certain examples, the ratios of sugars in the refined hemicellulose sugar stream are ideal for fermentation to xylitol, wherein enriching the concentration of xylose may reduce the efficiency and yield of the fermentation process. It is further realized that the high purity of the refined hemicellulose sugar stream is advantageous as feed for fermentation, as the concentrations of impurities known as possible fermentation inhibitors, such as phenols, furfurals, organic acids, and alcohols, is low.
A fermentation feedstock comprising the refined hemicellulose sugar stream can be utilized by a microorganism for the production of a conversion product. In some examples, the conversion product is a reduced sugar, such as a sugar alcohol. Optionally, the sugar alcohol may be a sugar substitute, such as xylitol. A schematic diagram of an exemplary process to convert a refined hemicellulose sugar stream to xylitol is provided in
The fermentation feedstock may have a very similar composition to the refined hemicellulose sugar stream. Optionally, additives are introduced to the refined hemicellulose sugar stream to generate the fermentation feedstock. Additives may be selected from nutrients, salts, such as NaCl, MgSO4, and K2PO4, and yeast extract. As such, measured ash levels may be higher in the fermentation feedstock as compared to the refined hemicellulose sugar stream. Optionally, hexoses are added to the refined hemicellulose sugar stream to adjust the xylose:hexose ratio as required for a particular microorganism. In some examples, the concentration of hemicellulose sugars is adjusted in the fermentation feedstock by dilution (e.g., dilution with water) or concentration (e.g., by evaporation).
The fermentation feedstock can comprise at least 40%, at least 45%, at least 50%, at least 55%, at least 60%, at least 65%, at least 70%, at least 75%, at least 80%, at least 90%, or at least 95% weight/weight xylose relative to total dissolved sugars. Optionally, the fermentation feedstock comprises between 40% and 95% weight/weight xylose relative to total dissolved sugars, such as 50% to 90% xylose. In some examples, the fermentation feedstock further comprises at least 5%, at least 10%, at least 12%, at least 15%, at least 17%, at least 20%, at least 22%, at least 25%, at least 27%, at least 30%, at least 32%, at least 35%, at least 37%, at least 40%, at least 42%, at least 45%, at least 50%, at least 52%, at least 55%, or at least 57% weight/weight hexoses relative to total dissolved sugars. Optionally, the fermentation feedstock comprises between 5% and 60% weight/weight hexoses relative to total dissolved sugars, such as 10% to 45% hexoses. In some examples, the fermentation feedstock further comprises less than 15%, less than 14%, less than 13%, less than 12%, less than 11%, less than 10%, less than 9%, less than 8%, less than 7%, less than 6%, less than 5%, less than 4%, less than 3%, or less than 2% weight/weight arabinose relative to total dissolved sugars. Optionally, the fermentation feedstock comprises between 1% and 15% weight/weight arabinose relative to total dissolved sugars, such as 3% to 12% arabinose. In some examples, the fermentation feedstock further comprises less than 15%, less than 10%, less than 9%, less than 8%, less than 7%, less than 6%, less than 5%, less than 4%, less than 3%, less than 2%, or less than 1% weight/weight disaccharides relative to total dissolved sugars. Optionally, the fermentation feedstock comprises between 0.1% and 15% weight/weight disaccharides relative to total dissolved sugars, such as 0.5% to 8% disaccharides. In some examples, the fermentation feedstock further comprises less than 1000 ppm, less than 750 ppm, less than 500 ppm, less than 400 ppm, less than 300 ppm, less than 200 ppm, less than 100 ppm, less than 50 ppm, or less than 10 ppm calcium. Optionally, the fermentation feedstock comprises between 1 ppm and 1000 ppm of calcium, such as 1 ppm to 250 ppm calcium. In some examples, the fermentation feedstock further comprises furfural in an amount up to 1000 ppm, up to 750 ppm, up to 500 ppm, up to 400 ppm, up to 300 ppm, up to 200 ppm, up to 100 ppm, up to 50 ppm, or up to 10 ppm. Optionally, the fermentation feedstock comprises between 1 ppm and 1000 ppm of furfural, such as 1 ppm to 250 ppm furfural. In some examples, the fermentation feedstock further comprises less than 1000 ppm, less than 750 ppm, less than 500 ppm, less than 400 ppm, less than 300 ppm, less than 200 ppm, less than 100 ppm, less than 50 ppm, or less than 10 ppm organic acids, such as acetic acid, levulinic acid, formic acid, and lactic acid. Optionally, the fermentation feedstock comprises between 1 ppm and 1000 ppm organic acids, such as 1 ppm to 1000 ppm acetic acid. Optionally, the fermentation feedstock comprises between 1 ppm and 1000 ppm of formic acid. In some examples, the fermentation feedstock further comprises an amine in an amount up to 1000 ppm, up to 750 ppm, up to 500 ppm, up to 400 ppm, up to 300 ppm, up to 200 ppm, up to 100 ppm, up to 50 ppm, or up to 10 ppm, and wherein the amine comprises at least 12 carbon atoms. Optionally, the amine is a laurylamine, such as monolaurylamine, dilaurylamine, or trilaurylamine. Optionally, the fermentation feedstock comprises between 0.1 ppm and 1000 ppm of an amine comprising at least 12 carbon atoms, such as 0.1 ppm to 250 ppm of an amine comprising at least 12 carbon atoms. In some examples, the fermentation feedstock further comprises a C6-12 monoalcohol in an amount up to 1000 ppm, up to 750 ppm, up to 500 ppm, up to 400 ppm, up to 300 ppm, up to 200 ppm, up to 100 ppm, up to 50 ppm, or up to 10 ppm. Optionally, the fermentation feedstock comprises between 1 ppm and 1000 ppm of said C6-12 monoalcohol, such as 1 ppm to 250 ppm of said C6-12 monoalcohol. In some examples, the fermentation feedstock further comprises nitrogen in an amount up to 1000 ppm, up to 750 ppm, up to 500 ppm, up to 400 ppm, up to 300 ppm, up to 200 ppm, or up to 150 ppm. Optionally, the fermentation feedstock comprises between 1 ppm and 1000 ppm of nitrogen, such as 1 ppm to 250 ppm nitrogen. In some examples, the fermentation feedstock comprises: 50% to 90% weight/weight xylose; 10% to 45% weight/weight hexoses; arabinose in an amount up to 12% weight/weight; disaccharides in an amount up to 8% weight/weight; furfural in an amount up to 1000 ppm; and less than 200 ppm calcium. In some examples, the fermentation feedstock further comprises less than 1000 ppm acetic acid and less than 1000 ppm formic acid. Optionally, the fermentation feedstock further comprises a C6-12 monoalcohol in an amount up to 100 ppm.
Various microorganisms have been developed to produce xylitol through a fermentation process. Surprisingly, the refined hemicellulose sugar streams of the present disclosure are particularly well tolerated by many such microorganisms and are efficiently converted to xylitol without the need for further purification, fractionation, separation, or crystallization processes prior to fermentation. Species of microorganisms capable of converting xylose in the refined hemicellulose sugar stream to xylitol include yeasts such as Pichia, Candida, Hansenula and Kluyveromyces. A strain of Candida tropicalis ATCC 13803 can be used for converting xylose to xylitol using glucose in the refined hemicellulose sugar stream for cell growth (see e.g. U.S. Pat. Nos. 5,998,181 and 5,686,277). Xylitol can be produced by Candida guilliermondii FTI 20037 (see e.g. Mussatto and Roberto (2003) J. Appl. Microbiol. 95:331-337). Saccharomyces cerevisiae can be used to produce xylitol (see e.g. U.S. Pat. No. 5,866,382). A variety of fermentation systems are able to convert a refined hemicellulose sugar stream to a high xylitol, low arabitol product, through the use of various strains of E. Coli (see e.g. PCT/US2011/021277, PCT/US2011/044696, and US Pub. No. 2013/0217070). These systems can utilize C6 sugars and some of the arabinose of a refined hemicellulose sugar stream as an energy source for proliferation and metabolism, while converting predominantly xylose to xylitol with minimal co-conversion of arabinose to arabitol. Optionally, the microorganism is a microorganism described in US Pub. No. 2013/0217070, such as HZ 1434, ZUC220, ZUC170, ZUC136, HZ 2061, or HZ 2062. A two-substrate fermentation with C. tropicalis and Candida Parapsilosis using glucose for cell growth and xylose for xylitol production can be used (see e.g. U.S. Pat. Nos. 5,998,181 and 5,686,277). Xylitol can be produced as a co-product during fermentative ethanol production by a single yeast strain, utilizing hydrolyzed lignocellulose-containing material (see e.g. US2003/0235881). Xylonic acid can be produced from xylose with a recombinant fungal strain that is genetically modified to express a xylose dehydrogenase gene, which is able to convert xylose to xylonolactone, coupled with xylitol production when the fungal host is selected from the genera Saccharomyces, Kluyveromyces, Candida and Aspergillus (see e.g. WO 2010/106230). While other genetically engineered organisms have been described to ferment xylose or a sugar mixture to produce xylitol, many show insufficient productivity to be viably commercialized. In some examples, the refined hemicellulose sugar stream (e.g., the fermentation feedstock) is fed into a fermentation unit seeded with the selected species at 10-40% DS, such as 14-28% DS. In some examples, the microorganism selectively reduces xylose to xylitol, without production of other polyols resulting from monosaccharides other than xylose in the fermentation broth.
The refined hemicellulose sugar stream can be added to a fermentation unit containing fermentation media. The fermentation media may comprise nutrients, including, for example, tryptone, yeast extract, potassium phosphate, sodium chloride, and magnesium sulfate. The fermentation unit can be inoculated with a culture of a suitable microorganism, optionally to a final concentration of 10-40% DS. In some examples, the temperature of the fermentation unit is maintained at a suitable temperature for the microorganism, such as 25 to 35° C. Optionally, the pH of the fermentation solution is maintained at pH 6.0 to pH 8.0, such as about pH 7.0. The pH can be adjusted using NH4OH. Optionally, the fermentation solution is agitated, such as by introduction of air. In some examples, additional refined hemicellulose sugar stream is added. In some examples, hexoses, such as glucose, are added to the fermentation solution. Additional refined hemicellulose sugar stream may be added 6 hours, 8 hours, 10 hours, 12 hours, 16 hours, 20 hours, 24 hour, 36 hours, or 48 hours after addition of the microorganism to the fermentation unit. The fermentation process may be allowed to run for at least 12 hours, at least 18 hours, at least 24 hours, at least 36 hours, at least 48 hours, at least 60 hours, at least 72 hours, at least 80 hours, at least 84 hours, at least 96 hours, or at least 108 hours before recovering xylitol from the fermentation broth.
A microorganism described herein can convert the fermentation feedstock into a fermentation broth comprising xylitol. The fermentation broth can comprise at least 50 g/L, at least 60 g/L, at least 70 g/L, at least 80 g/L, at least 90 g/L, at least 100 g/L, at least 110 g/L, at least 120 g/L, at least 130 g/L, or at least 140 g/L xylitol. Optionally, the fermentation broth comprises between 50 and 140 g/L xylitol, such as 60 to 100 g/L, 70 to 100 g/L, 80 to 100 g/L, or 70 to 90 g/L xylitol. In some examples, the microorganism produces little to no ethanol. Optionally, the fermentation broth comprises less than 15 g/L, less than 12 g/L, less than 10 g/L, less than 9 g/L, less than 8 g/L, less than 7 g/L, less than 6 g/L, less than 5 g/L, less than 4 g/L, less than 3 g/L, less than 2 g/L, or less than 1 g/L ethanol. In some examples, the fermentation broth comprises xylose in an amount less than 50 g/L, less than 40 g/L, less than 30 g/L, less than 20 g/L, less than 10 g/L, less than 8 g/L, less than 6 g/L, less than 4 g/L, less than 3 g/L, less than 2 g/L, less than 1 g/L, less than 0.5 g/L, or less than 0.2 g/L. Optionally, the fermentation broth comprises glucose in an amount less than 35 g/L, less than 25 g/L, less than 15 g/L, less than 10 g/L, less than 8 g/L, less than 6 g/L, less than 4 g/L, less than 3 g/L, less than 2 g/L, less than 1 g/L, less than 0.5 g/L, or less than 0.2 g/L. In some examples, the fermentation broth comprises furfural in an amount up to 1000 ppm, up to 750 ppm, up to 500 ppm, up to 400 ppm, up to 300 ppm, up to 200 ppm, up to 100 ppm, up to 50 ppm, or up to 10 ppm. Optionally, the fermentation broth comprises between 1 ppm and 1000 ppm of furfural, such as 1 ppm to 250 ppm furfural. In some examples, the fermentation broth comprises less than 1000 ppm, less than 750 ppm, less than 500 ppm, less than 400 ppm, less than 300 ppm, less than 200 ppm, less than 100 ppm, less than 50 ppm, or less than 10 ppm calcium. Optionally, the fermentation broth comprises between 1 ppm and 1000 ppm of calcium, such as 1 ppm to 250 ppm calcium. In some examples, the fermentation broth comprises less than 1000 ppm, less than 750 ppm, less than 500 ppm, less than 400 ppm, less than 300 ppm, less than 200 ppm, less than 100 ppm, less than 50 ppm, or less than 10 ppm organic acids, such as acetic acid, levulinic acid, formic acid, and lactic acid. Optionally, the fermentation broth comprises between 1 ppm and 1000 ppm organic acids, such as 1 ppm to 1000 ppm acetic acid. Optionally, the fermentation broth comprises between 1 ppm and 1000 ppm of formic acid. In some examples, the fermentation broth comprises a C6-12 monoalcohol in an amount up to 1000 ppm, up to 750 ppm, up to 500 ppm, up to 400 ppm, up to 300 ppm, up to 200 ppm, up to 100 ppm, up to 50 ppm, or up to 10 ppm. Optionally, the fermentation broth comprises between 1 ppm and 1000 ppm of said C6-12 monoalcohol, such as 1 ppm to 250 ppm of said C6-12 monoalcohol. In some examples, the fermentation broth comprises: at least 60 g/L xylitol; less than 50 g/L xylose; less than 10 g/L ethanol; less than 50 g/L hexoses; furfural in an amount up to 1000 ppm; and less than 200 ppm calcium. In some examples, the fermentation broth further comprises less than 1000 ppm acetic acid and less than 1000 ppm formic acid. Optionally, the fermentation broth further comprises a C6-12 monoalcohol in an amount up to 100 ppm. Optionally, the fermentation broth comprises less than 100 ppm galactitol, such as less than 50 ppm, less than 10 ppm, less than 1 ppm, or less than 1 ppb galactitol. In some examples, galactitol is not detected in the fermentation broth. In some examples, the fermentation broth comprises a microorganism described herein. Optionally, the microorganism is selected from naturally occurring bacteria, recombinant bacteria, naturally occurring yeast, recombinant yeast, and fungi. The microorganism may be an E. coli strain, such as such as HZ 1434, ZUC220, ZUC170, ZUC136, HZ 2061, or HZ 2062.
Optionally, the yield of xylitol in the fermentation broth is more than 90%, more than 91%, more than 92%, more than 93%, more than 94%, more than 95%, more than 96%, more than 97%, or more than 98% of relative to the amount of xylose in the refined hemicellulose sugar stream. In some examples, at least 70%, at least 75%, at least 80%, at least 85%, at least 90%, at least 91%, at least 92%, at least 93%, at least 94%, at least 95%, at least 96%, at least 97%, or at least 98% of xylose in the lignocellulose containing biomass is converted to xylitol. Optionally, the amount of arabitol in the fermentation broth is less than 10% of the total polyols. Optionally, the amount of hexoses is reduced to less than 10%, less than 9%, less than 8%, less than 7%, less than 6%, less than 5%, less than 4%, less than 3%, less than 2%, or less than 1% of the concentration of hexoses in the fermentation feedstock or refined hemicellulose sugar stream. Optionally, the fermenting produces xylitol at a rate of at least 1 g/L/h, at least 2 g/L/h, at least 3 g/L/h, at least 4 g/L/h, at least 5 g/L/h, at least 6 g/L/h, at least 7 g/L/h, or at least 8 g/L/h. In some examples, the fermenting produces—in less than 120 h, less than 110 h, less than 100 h, less than 90 h, less than 80 h, less than 70 h, less than 60 h, less than 50 h, less than 40 h, less than 30 h, less than 20 h, less than 15 h, or less than 10 h-at least 50 g/L, at least 60 g/L, at least 70 g/L, at least 80 g/L, at least 90 g/L, at least 100 g/L, at least 110 g/L, at least 120 g/L, at least 130 g/L, or at least 140 g/L xylitol (per liter of fermentation broth). Optionally, the fermenting produces at least 60 g/L xylitol in less than 80 hours of fermenting, such as 70 g/L xylitol in less than 80 hours. Optionally, the fermenting produces at least 100 g/L xylitol in less than 80 hours of fermenting.
Xylitol can be recovered from the fermentation broth by any suitable method (1910), such as filtration, crystallization, or chromatographic separation, or a combination thereof. The fermentation broth can be filtered or centrifuged to remove the microorganism. In some examples, filtration comprises three steps, including microfiltration, ultrafiltration, and nanofiltration. The fermentation broth may be subjected to microfiltration, optionally followed by ultrafiltration, optionally followed by nanofiltration. The filtration can remove the microorganism from the fermentation broth. The nanofiltration can remove residual disaccharides and oligosaccharides from the fermentation broth. In some examples, the filtration removes at least 10%, at least 20%, at least 30%, at least 40%, at least 50%, at least 60%, at least 70%, at least 80%, at least 90%, at least 95%, or at least 98% weight/weight oligosaccharides having a degree of polymerization of three (DP3) or more from the fermentation broth. In some examples, the filtration removes at least 10%, at least 20%, at least 30%, at least 40%, at least 50%, at least 60%, at least 70%, at least 80%, at least 90%, at least 95%, or at least 98% weight/weight disaccharides (DP2) from the fermentation broth. The filtered solution can be contacted with at least one of the following: activated carbon, such as granulated active carbon (GAC); and ion exchange resin, such as strongly acidic cation (SAC) resin, weakly basic anion (WBA) resins, and mixed bed (MB) resins. The filtered and optionally refined solution can be concentrated by evaporation (1915) to increase the concentration of dissolved solids to at least 50%, at least 60%, at least 70%, or at least 80% weight/weight dissolved solids, such as about 80% weight/weight dissolved solids. In some examples, the concentration of the solution is about 70% to about 90% weight/weight dissolved solids, such as 75% to 85% weight/weight.
The solution can be introduced batch-wise or continuously into a xylitol crystallization unit (1920). Optionally, ethanol is added to a specified concentration, such as 0-40% weight/weight ethanol. Optionally, the solution is seeded with xylitol crystals and cooled gradually at a controlled rate under agitation to induce crystallization. Xylitol crystals can be collected by filtration or centrifugation. Optionally, the collected xylitol crystals are washed and dried (1960). Optionally, the collected xylitol crystals are re-dissolved (1940) to form a xylitol solution. The xylitol solution may be further polished (1950) and the polished solution used as liquid xylitol product (1950-A). Polishing may include contacting the xylitol solution with an ion exchange resin, such as SAC, WBA, and MB resins. Optionally, polishing includes contacting the xylitol solution with granulated active carbon.
The mother liquor of the xylitol crystallization can be concentrated by evaporation (1922) to at least 70% weight/weight dissolved solids, such as 80% to 88% weight/weight dissolved solids. Optionally, the mother liquor is stripped by evaporation to remove ethanol, if present (1928). The concentrated mother liquor can be introduced into a second xylitol crystallization unit (1925) and can optionally be seeded with xylitol crystals. Gradual cooling at a controlled rate may result in a second crystallization of xylitol. These crystals (1925-A) can be collected by filtration or centrifugation. The second crystallization may yield crystals of lower purity than the first crystallization. In some examples, the mother liquor of the second crystallization is separated by chromatography (1930) to yield an extract stream comprising a composition similar to the first mother liquor, a raffinate stream which is low in xylitol and rich in arabitol, and a third stream comprising residual reducing sugars and residual oligomers. The extract stream can be recycled into the second crystallization unit to increase overall xylitol yield. Optionally, the extract stream is stripped by evaporation to remove ethanol, if present. Optionally, the third stream comprising residual reducing sugars is recycled to fermentation. Optionally, the third stream is stripped by evaporation to remove ethanol, if present (1935). Optionally, the raffinate stream comprising arabitol is fed into an anaerobic digester to convert the organic matter to methane that can be used as an energy source. Optionally, the raffinate stream is stripped by evaporation to remove ethanol, if present (1936).
In some examples, recovering xylitol from the fermentation broth comprises: (i) filtering the fermentation broth through a microfilter and collecting the resulting microfiltrate; (ii) filtering the microfiltrate through an ultrafilter and collecting the resulting ultrafiltrate; (iii) filtering the ultrafiltrate through a nanofilter and collecting the resulting nanofiltrate; (iv) contacting the nanofiltrate with an ion exchange resin, thereby producing a refined nanofiltrate; (v) concentrating the refined nanofiltrate by evaporation, thereby producing a concentrated nanofiltrate; (vi) crystallizing xylitol from the concentrated nanofiltrate; and (vii) separating xylitol crystals from the mother liquor. Optionally, recovering xylitol from the fermentation broth further comprises: (viii) dissolving the xylitol crystals to form a xylitol solution; and (ix) polishing the xylitol solution with an ion exchange resin.
Recovered xylitol product can comprise at least 95% weight/weight xylitol, such as at least 96%, at least 97%, at least 98%, at least 99%, at least 99.5%, or at least 99.9% weight/weight xylitol. The xylitol product can be produced by a method described herein. Optionally, the xylitol product comprises less than 1% weight/weight oligosaccharides, such as less than 0.5%, less than 0.25%, less than 0.1%, less than 0.05%, or less than 0.01% weight/weight oligosaccharides. Optionally, the xylitol product comprises hexoses in an amount up to 1% weight/weight, such as up to 0.5%, up to 0.25%, up to 0.1%, up to 0.05%, or up to 0.01% weight/weight hexoses. The hexoses may be selected from glucose, galactose, mannose, and fructose. Optionally, the xylitol product comprises less than 100 ppm arabitol, such as less than 50 ppm, 10 ppm, 1 ppm, or 1 ppb arabitol. Optionally, the xylitol product comprises less than 100 ppm galactitol, such as less than 50 ppm, 10 ppm, 1 ppm, or 1 ppb galactitol. In some examples, galactitol is not detected in the xylitol product. Optionally, the xylitol product comprises ash in an amount up to 0.25% weight/weight, such as up to 0.1%, up to 0.05%, or up to 0.01% weight/weight ash. Optionally, the xylitol product comprises furfural in an amount up to 500 ppm, such as up to 250 ppm, 100 ppm, 50 ppm, 10 ppm, or 1 ppm furfural. Optionally, the xylitol product comprises an amine in an amount up to 500 ppm, such as up to 250 ppm, 100 ppm, 50 ppm, 10 ppm, or 1 ppm amine, and wherein the amine comprises at least 12 carbon atoms. Optionally, the xylitol product comprises a C6-12 monoalcohol in an amount up to 500 ppm, such as up to 250 ppm, 100 ppm, 50 ppm, 10 ppm, or 1 ppm C6-12 monoalcohol. In some examples, the xylitol product is provided in crystalline form. In some examples, the xylitol product is provided as an aqueous solution. Optionally, the concentration of the aqueous solution is at least 50% weight/weight dissolved solids, for example, about 70% to about 90% weight/weight dissolved solids, such as 75% to 85% weight/weight.
The overall recovery yield of xylitol by a xylitol separation of the subject methods can be more than 70%, more than 75%, more than 80%, more than 85%, more than 86%, more than 87%, more than 88%, more than 89%, more than 90%, more than 91%, more than 92%, more than 93%, more than 94%, more than 95%, more than 96%, more than 97%, or more than 98% xylitol. In some examples, the yield of xylitol recovered by the subject methods is at least 50%, at least 55%, at least 60%, at least 65%, at least 70%, at least 75%, at least 80%, at least 85%, at least 90%, at least 91%, at least 92%, at least 93%, at least 94%, at least 95%, at least 96%, at least 97%, or at least 98% xylitol relative to the xylose content of the lignocellulose containing biomass.
Xylitol can be separated from a sugar mixture solution by simulated moving bed (SMB) ion exclusion chromatography using anion exchange resin (see e.g. U.S. Pat. No. 6,451,123). An improved system and method for the fractionation of xylitol by an industrial scale sequential simulated moving bed (SSMB) chromatography can be used (see e.g. U.S. application Ser. No. 14/398,444). Alternatively, a SAC resin can be used for the separation of xylitol from a polyol mixture (see e.g. U.S. Pat. No. 4,008,285), wherein the salt of the resin is selected from the group consisting of alkaline earth metal salts (e.g. Sr2+ salts, Ca2+ salts), Fe3+ salts and Al3+ salts. In some examples, a similar SSMB method is applied to yield a xylitol enriched stream, an arabitol stream and a reducing sugar stream comprising monomers and oligomers. The xylitol enriched stream is recycled to the crystallizer feed, such that yield of xylitol is maximized. The reducing sugar stream is optionally stripped of residual ethanol, if present, and recycled to the fermentation unit. The arabitol stream is stripped of residual ethanol, if present, and is fed to a waste treatment process comprising an anaerobic digester to produce methane that can be used as an energy source for the process.
A chromatographic fractionation to achieve enrichment of xylitol concentration can be carried out with ion exchange resins (e.g., a cation exchange resin and an anion exchange resin) as the column packing material. Cation exchange resins include strong acid cation exchange resins and weak acid cation exchange resins. The strong acid cation exchange resins can be in a monovalent or multivalent metal cation form, e.g., in H+, Mg2+, Ca2+, Sr2+ or Zn2+ form. The strong acid cation exchange resins typically have a styrene skeleton, which is preferably cross-linked with 3 to 8%, preferably 5 to 6.5% of divinylbenzene. The weak acid cation exchange resins may be in a monovalent or multivalent metal cation form, e.g., H+, Mg2+, Ca2+, Sr2+ form, or Na+ form. Suitable resins can be purchased from Lanxess AG, Purolite, Dow Chemicals Ltd. or Rohm & Haas.
A chromatographic fractionation can be carried out in a batch mode, a simulated moving bed (SMB) mode, or a sequential simulated moving bed (SSMB) mode. The temperature of the chromatographic fractionation is typically in the range of 20 to 90° C., such as 40 to 65° C. The pH of the solution to be fractionated can be acidic or adjusted to a range of pH 2.5 to 7, preferably 3.5 to 6.5, and most preferably 4 to 5.5. The fractionation can be carried out with a linear flow rate of about 1 m/h to about 10 m/h in the separation column.
A biomass embodied in a subject method or system disclosed herein may be sugarcane bagasse. In some examples, the biomass may comprise sugarcane leaves. While it may be desirable to return some mass of sugarcane leaves back to the soil after harvest, excess mass of sugarcane leaves may be problematic. Many skilled in the art currently consider sugarcane leaves to be waste that needs to be treated, often in environmentally unfriendly solutions such as burning. Sugarcane leaves that enter the sugar mill can reduce production capacity and increase sucrose losses to the exiting fiber (i.e., bagasse). It can be therefore advantageous to the sugarcane growers and/or the sugar mill to use leaves as a source of hemicellulosic sugars. Currently, some of the leaves can be processed through the sugar mill. Since sucrose content in the leaves is low, they effectively reduce the productivity of the sugar mill. In some examples, leaves are separated from the harvested canes by air classification to separate the light leaves from the heavy cane. In some examples, the leaves are collected in the field, baled and then transferred directly to the wash unit for processing. Sugarcane leaves may be processed similarly to sugarcane bagasse or blended with bagasse for processing.
If a high xylose feedstock other than sugarcane bagasse or leaves is used, e.g. birch or eucalyptus, the wash step may be unnecessary and the system adapted accordingly by replacing the wash unit with a debarking and sizing system. The hemicellulose extraction units and methods disclosed herein are particularly suitable for recovering hemicellulose sugars comprising xylose from pre-hydrolysates produced at dissolving pulp mills in the production of cellulosic fibers, e.g. viscose and acetate. Pre-hydrolysis is applied at dissolving pulp mills to remove hemicellulose from the biomass prior to a Kraft or sulfite pulping. Dissolving pulps typically contain low levels of residual hemicellulose (e.g., up to 3%, up to 2% or up to 1% weight/weight hemicellulose), compared to higher levels in typical paper grade Kraft pulp, typically about 10%. Typically, pre-hydrolysis is conducted in diffusing pulp digesters by treating the wood chips with steam or water to induce autohydrolysis. Steam hydrolysis can result in the hydrolysate being held by the wood pores. Hydrolysis in water can allow for collection of the formed hydrolysate in higher yields. Optionally, an acid may be added to the water to accelerate hemicellulose hydrolysis. Optionally, the acid may be a mineral acid or an organic acid, e.g. SO2, H2SO4, HCl, acetic acid, or formic acid. Since pre-hydrolysis conditions can be fairly severe to optimally remove hemicellulose from the biomass, the resulting hydrolysate can be relatively high in degradation products. Nonetheless, the hydrolysate can be refined and xylose and/or xylitol can be harvested in the systems and methods disclosed herein, thus valorizing the hydrolysate stream and contributing significantly to the economics of the mill. Optionally, the system disclosed herein can be combined with the dissolving pulp mill for recovery of chemicals, solvent recycling, and harvesting of energy from waste streams, thus reducing production cost of both the hemicellulose sugars and the dissolving pulp. Optionally, hexoses are added to the hydrolysate prior to fermentation to achieve the preferred ratios of xylose to hexoses as described above for the refined hemicellulose sugar stream and the fermentation feedstock.
In one aspect, the disclosure provides a system for producing xylitol from a lignocellulose-containing biomass. In one example, the system comprises: (i) a hemicellulose extraction unit configured to extract and hydrolyze hemicellulose from the biomass to produce a hemicellulose sugar stream and a lignocellulose remainder stream; (ii) a refining unit in fluid communication with the extraction unit, wherein the refining unit is configured to receive the hemicellulose sugar stream and an amine extractant, and wherein the amine extractant removes impurities from the hemicellulose sugar stream to produce a refined hemicellulose sugar stream; optionally, (iii) a sensing unit configured to analyze one or more parameters of the refined hemicellulose sugar stream, wherein the one or more parameters are selected from pH, light absorbance, conductivity, density, xylose concentration, and hexose concentration; (iv) a fermentation unit in fluid communication with the refining unit to receive the refined hemicellulose sugar stream, wherein the fermentation unit is configured to contain the refined stream and a microorganism, and wherein the microorganism facilitates production of the xylitol from a monosaccharide in the refined stream to produce a fermentation broth; and (v) a xylitol refining unit, wherein the xylitol refining unit is configured to remove the xylitol from the fermentation broth.
Optionally, the system further comprises a wash unit configured to remove ash and soil from the biomass. The wash unit can be in fluid communication with the hemicellulose extraction unit. Optionally, a counter current wash unit as depicted in
Each stage of a wash unit used to reduce soil and ash content of a biomass may comprise a tank, wherein the biomass is re-slurried by means of a stirrer, a pump or any other means capable of causing re-slurry of the biomass in water. Optionally, the ratio of liquid to solid in the tank is 30-60:1, such as a liquid to solid ratio of 60 to 1, 55 to 1, 50 to 1, 45 to 1, 40 to 1, 35 to 1, or 30 to 1. Each tank may be equipped with a solids inlet. The tank may be in fluid communication, e.g. via a pump and a pipe, with a dewatering device, wherein the slurry in the tank can be transferred to the dewatering device. The wash unit may comprise a pipe to return the liquid phase from the dewatering device to the tank. Optionally, the dewatering device is positioned higher than the tank so that gravity can assist return of the liquid to the tank. In some examples, each tank is equipped with a liquid inlet connected to receive liquid from its n+1 stage, and a liquid outlet connected to deliver liquid to its n−1 stage, where the liquid outlet of stage I can be connected to deliver liquid to an auxiliary tank for water recycling. The position of the liquid outlet can be at the top of the liquid phase in the tank of each stage, such that liquid is transferred as an overflow stream. Optionally, the tank of stage n comprises an additional water inlet connected to receive a water stream. Optionally, the water stream comprises recycled filtered or treated water from the wash unit, fresh water, or process water from other units of the system.
An auxiliary tank of the wash unit may receive a purge stream. The purge stream may come from the sequential overflow or from the bottom purge of the tanks, in a continuous or intermittent mode. Optionally, the auxiliary tank is connected to at least one device for the separation of fine particles from the liquid, such as a hydrocyclone, a centrifuge, or a filter. A hydrocylone or a centrifuge may be used to recover fine biomass particles from the top outlet. This recovered biomass can be sent to the tank of stage n to minimize biomass losses. Ash and soil particles can be separated from the bottom outlet or the higher density outlet (however positioned in the separation device used). This stream can be further filtered to remove soil and recover the water.
The tank of each stage may also be equipped with a low level liquid/solid outlet, preferably positioned at the bottom of the tank. Optionally, the system is also equipped with at least one inlet of pressurized air. One or more stages may be equipped with a grinding or milling device, wherein such device is optionally an inline or submerged grinding or milling device. In some examples, the grinding or milling is increasingly finer with each progressive stage n in the wash unit. Various vendors offer suitable grinding, milling, homogenizing and pulping devices, including, for example, EBERA Fluid Handling, Bolton Emerson, ARDE-BARINKO and IKA. Different devices may be used at different stages.
Optionally, at least one dewatering device comprises a screen. The screen size may vary between 1000 and 100 micrometers. Optionally, the size of the screen is decreased with each progressive stage m in the wash unit. The screen can be held in a diagonal position or a bent position with respect to earth. Biomass can be collected from the top of the screen and transferred through a solid transfer chute to the tank of stage n+1. A liquid comprising soil particles and fine particles of biomass may go through the screen and can be returned to the tank of stage n. Various vendors offer suitable screening devices, including, for example, Dorr-Oliver and FluidQuip. Different devices may be used at different stages.
In some examples, a dewatering device may be connected to another dewatering device directly (i.e. not through another tank). Optionally, the final dewatering device m applies pressure to reduce water content to a minimum. In some examples, the final water content of the washed biomass may be less than 70, less than 65, less than 60, less than 55, less than 50, less than 45, less than 40, less than 35, or less than 30% wt/wt. In some examples, the final water content of the washed biomass is 40-60% wt/wt. The final dewatering device may comprise a screw press. A suitable screw press can comprise either a single or double screw or a twin screw or roller mill that achieves the final water content at the desired production rate. Various vendors offer suitable screw press devices, including, for example, Vincent Corporation, Stord Bartz, FKC Company Ltd and Parkson Corporation. Different devices may be used at different stages.
Raw biomass can be received by the wash unit from harvest or upstream treatment in chips, lumps, or particles of various sizes. Optionally, the raw biomass is first crushed or shredded to break up lumps and to size the raw biomass to uniform size that can be re-slurried and handled by pumps and mills further downstream. Suitable systems for crushing or shredding may be selected from, but are not limited to, a jaw crusher, a cone crusher, a tub grinder, a hammer mill, and a chipper. Numerous vendors offer such equipment, including, for example, West Salem Machinery, Metso Corporation and Andritz. Optionally, the raw biomass is sized such that greater than 70, 75, 80, 81, 82, 83, 84, 85, 86, 87, 88, 89, 90, 91, 92, 93, 94, 95, 96, 97, 98, or greater than 99% weight/weight goes through a mesh 20 sieve (841 micrometer). Optionally, the raw biomass is sized such that greater than 70, 75, 80, 81, 82, 83, 84, 85, 86, 87, 88, 89, 90, 91, 92, 93, 94, 95, 96, 97, 98, or greater than 99% weight/weight goes through a mesh 12 sieve (1680 micrometer). Optionally, the raw biomass is sized such that greater than 70, 75, 80, 81, 82, 83, 84, 85, 86, 87, 88, 89, 90, 91, 92, 93, 94, 95, 96, 97, 98, or greater than 99% weight/weight goes through a mesh 7 sieve (2830 micrometer). Optionally, the raw biomass is sized such that greater than 70, 75, 80, 81, 82, 83, 84, 85, 86, 87, 88, 89, 90, 91, 92, 93, 94, 95, 96, 97, 98, or greater than 99% weight/weight goes through a mesh 5 sieve (4000 micrometer). In some examples, greater than 93% wt/wt goes through a mesh 12 sieve and greater than 90% wt/wt goes through a mesh 20 sieve. In some examples, about 20% (wt/wt) of the material is retained on a mesh 60 sieve (250 micrometer) and about 20% (wt/wt) is retained on a mesh 40 sieve (400 micrometer). In some examples, less than 4%, less than 5%, less than 6%, less than 7%, less than 8%, less than 9%, less than 10%, less than 11%, or less than 12% weight/weight goes through a mesh 200 sieve (74 micrometer). The sized raw biomass can be transferred by any means of transferring solid material and can be fed to the tank of stage I of the wash unit.
A system described herein may comprise a hemicellulose extraction unit configured to extract and hydrolyze hemicellulose from biomass to produce a hemicellulose sugar stream and a lignocellulose remainder stream. A hemicellulose extraction unit may comprise a tank equipped with a solid feed device and at least one aqueous feed device, wherein the tank can hold pressure of at least 400 psi and can be heated to temperature of at least 250° C. The tank can be equipped with stirring capability to mix solid and liquid streams. Optionally, the tank is equipped with flow capability to move solid and liquid streams. The tank can be equipped with an outlet suitable for removing the reacted slurry. A tank of the extraction unit can optionally have more than one compartment wherein adjacent compartments are separated by weirs. Optionally, the extraction unit may comprise more than one tank, wherein the tanks are in fluid communication with adjacent tanks to allow for mass flow through consecutive tanks. In some examples, the extraction unit comprises a plug flow reactor. The plug flow reactor may be mounted at a low angle to assist in reactor emptying when a shutdown is required. The reactor can be partially or fully jacketed to prevent heat loss.
An aqueous slurry comprising the biomass may be fed continuously to the hemicellulose extraction unit. In some examples, acid concentration of the aqueous slurry is monitored. Optionally, additional acid is added if the acid concentration is below a threshold. Optionally, said monitoring is continuous and said acid addition is controlled by a computerized system that accepts input from at least one probe, wherein the computerized system further controls pumps and valves of the system. Optionally, the extraction product, e.g., a hemicellulose extraction slurry comprising hemicellulose sugars, is removed continuously. In some examples, the aqueous slurry fed to the extraction unit can be heated in the incoming stream. Optionally, the slurry is heated in a tank of the extraction unit. In some examples, a stream exiting the extraction unit (e.g., a hemicellulose extraction slurry) is cooled. Heating or cooling processes may be fast, e.g., flash heating and/or flash cooling. Optionally, heating to the extraction set point is done in less than 60, less than 45, less than 30, less than 25, less than 20, less than 15, less than 10, or less than 5 minutes. Optionally, cooling of the extraction slurry is done in less than 60, less than 45, less than 30, less than 25, less than 20, less than 15, less than 10, or less than 5 minutes. Heat removed at the cooling end can be used to heat the heating end by the use of suitable heat exchangers, e.g. spiral type shell and tube, standard shell and tube or a plate and frame. Suitable heat exchangers can be obtained, for example, from Alfa Laval or Chemineer Inc. In some examples, the extraction unit is used to conduct a batch or preferably a continuous process to extract hemicellulose, organic acids and remaining ash and extractives from biomass.
In some examples, the hemicellulose extraction slurry comprises hemicellulose sugars and lignocellulose remainder. The hemicellulose extraction unit may comprise a system for separating a lignocellulose remainder stream from the hemicellulose sugar stream. Optionally, the lignocellulose remainder stream is washed to remove residual hemicellulose sugars. Optionally, the hemicellulose sugar stream is washed to remove residual lignocellulose components. A system for separating solids, such as the lignocellulose remainder stream, from liquids, such as the hemicellulose sugar stream, following hemicellulose extraction is presented in
The lignocellulose remainder stream may be separated from the hemicellulose sugar stream by means of a vacuum belt filter. Vacuum belt filter systems are commercially available from various suppliers, including, for example, Pannevis, BHS-Sonthofen Inc. and FLSmidth. In some examples, the extraction slurry is continuously fed over a moving belt. As the belt moves, vacuum may be applied to remove liquids and create a filtration cake resting on the moving belt. Optionally, the belt passes through a wash zone. Optionally, the belt passes through a drying zone. A wash zone may comprise nozzles that spray a wash fluid on the filtration cake (i.e., the lignocellulose remainder stream) to rinse residual hemicellulose sugars from the lignocellulose remainder stream, thereby increasing the recovery of hemicellulose sugars. The temperature of the extraction slurry and wash fluid may be about 20-100° C., such as 30-90° C., 35-85° C., 35-80° C., 40-80° C., 50-80° C., 40-75° C., or 55-75° C. Optionally, the wash fluid is water. The flow of the wash fluid can be about 0.25, 0.3, 0.4, 0.5, 0.6, 0.7, 0.8, 0.9, or 1 compared to the flow of the extraction slurry. In some examples, less than 40%, less than 30%, less than 20%, less than 10%, less than 5%, less than 4%, less than 3%, less than 2.5%, less than 2%, less than 1.5%, or less than 1% of the solids remain in the hemicellulose sugar stream. In some examples, the belt is rolled over a roller to cause the filtration cake (i.e., the lignocellulose remainder stream) to fall off. Optionally, residual solids are scraped off the belt with scrapers. More than about 60%, more than about 70%, more than about 80%, more than about 90%, or more than about 95% of the solids in the extraction slurry can be recovered in the lignocellulose remainder stream. After removal of the lignocellulose remainder stream, the belt may be rolled back to the starting rollers at the beginning of the line. A vacuum belt may be fabricated of various materials using different methods of cloth production and may be woven or non-woven. Fabrication may be optimized to produce the desired porosity, thickness, and air permeability.
A system described herein may comprise a refining unit in fluid communication with the extraction unit, wherein the refining unit is configured to receive the hemicellulose sugar stream and an amine extractant, and wherein the amine extractant removes impurities from the hemicellulose sugar stream to produce a refined hemicellulose sugar stream. Optionally, the hemicellulose sugar stream is extracted with an amine extractant counter-currently, e.g., the hemicellulose sugar stream flows in a direction opposite to the flow of the amine extractant. The refining unit may comprise a mixer-settler device, a stirred tank, a liquid-liquid separation centrifuge, or a column, wherein the mixer-settler device, stirred tank, liquid-liquid separation centrifuge, or column is equipped with a liquid feed device to receive the hemicellulose sugar stream from the extraction unit. The refining unit can be equipped with an inlet to receive the amine extractant. Optionally, the amine extraction is conducted in a mixer-settler device, wherein the mixer-settler device can be designed to minimize emulsion formation, thereby reducing phase separation time. A mixer-settler may comprise a first stage that mixes the phases together followed by a quiescent settling stage that allows the phases to separate by gravity. Various mixer-settlers known in the art can be used. In some examples, phase separation may be enhanced by incorporating a suitable centrifuge with the mixer-settler. Optionally, both mixing and separation may be conducted in a liquid-liquid separation centrifuge. Liquid-liquid separation centrifuges are commercially available from various suppliers, including, for example, Rousselet Robatel Inc. and US Centrifuge Systems LLC. The amine extraction can be conducted at any temperature at which the amine is soluble, such as 50-70° C. Optionally, the amine extraction comprises more than one extraction step (e.g., 2, 3, or 4 steps). The ratio of the amine extractant stream (organic stream) to the hemicellulose sugar stream (aqueous stream) can range from about 0.5:1 to about 5:1 weight/weight, such as about 0.5:1, about 1:1, about 1.5:1, about 2:1, about 2.5:1, about 3:1, about 3.5:1, about 4:1, about 4.5:1, or about 5:1. In some examples, the ratio of the organic stream to the aqueous stream is about 1.5-4.0:1 weight/weight. The refining unit may further comprise at least one outlet for removing the refined hemicellulose sugar stream. In some examples, the refining unit further comprises column or batch units for contacting the hemicellulose sugar stream with ion exchange resins or activated carbon to further polish the refined sugar solution. In some examples, the outlet is in fluid communication with a fermentation unit. The refining unit may comprise second outlet for removing the organic stream comprising the amine extractant. In some examples, the organic stream is treated and the resultant purified amine extractant recycled back to the refining unit.
A system described herein may comprise a sensing unit in fluid communication with the refining unit to analyze the refined hemicellulose sugar stream. The sensing unit may analyze the refined hemicellulose sugar stream continuously or in batches. In some examples, the sensing unit comprises a pH probe. Optionally, if the pH probe detects that the pH of the refined hemicellulose sugar stream is too acidic, such as pH less than about 3.0, the sensing unit may divert the stream away from the fermentation unit. In some examples, if a pH probe detects that the pH of the refined hemicellulose sugar stream is too acidic, the sensing unit is configured to raise the pH of the solution, for example, by addition of ammonia. In some examples, the sensing unit analyzes color of the refined hemicellulose sugar stream, for example, using a spectrophotometer. If the light absorbance at a particular wavelength is determined to be too high, the sensing unit may divert the stream away from the fermentation unit. In some examples, the sensing unit analyzes conductivity of the refined hemicellulose sugar stream, for example, using a conductivity probe. If the conductivity is determined to be too high, such as conductivity greater than 10,000 microS/cm, the sensing unit may divert the stream away from the fermentation unit. In some examples, the sensing unit analyzes density of the refined hemicellulose sugar stream, for example, using a refractometer. If the density is determined to be too high or too low, such as a density corresponding to a sugar concentration outside the range of 50 g/L to 300 g/L, the sensing unit may divert the stream away from the fermentation unit, or may cause the addition of water to dilute the stream. The sensing unit may be configured to analyze concentration of one or more components of the refined hemicellulose sugar stream, wherein the one or more components are selected from xylose, arabinose, hexoses, glucose, galactose, mannose, fructose, disaccharides, oligosaccharides, ash, phenolic compounds, furfural, and hydroxymethylfurfural. Any concentration outside the ranges described for the subject methods and compositions may cause the sensing unit to divert the stream away from the fermentation unit, or to correct the concentration by suitable compensation or dilution. Any stream diverted from the fermentation unit may be further refined or utilized in some other process of the plant.
A system described herein may comprise a fermentation unit in fluid communication with the refining unit to receive the refined hemicellulose sugar stream, wherein the fermentation unit is configured to contain a fermentation feedstock comprising the refined stream and a microorganism, wherein the microorganism facilitates production of the xylitol from a monosaccharide in the refined hemicellulose sugar stream to produce a fermentation broth. The fermentation unit may comprise a tank equipped with at least one aqueous feed inlet to receive the refined hemicellulose sugar stream. Optionally, the fermentation unit can be temperature controlled, such that the fermentation unit maintains a given fermentation temperature within ±10° C., within ±8° C., within ±5° C., within ±4° C., within ±3° C., or within ±2° C. Optionally, the fermentation unit comprises one or more sensors, such as a temperature sensor, a density sensor, or a pH sensor. Optionally, the fermentation unit comprises a density sensor, such as a refractometer, such that the specific gravity of the fermentation broth can be measured. A change in the density of the fermentation broth above or below a certain threshold may indicate that the fermentation has consumed a desired concentration of hemicellulose sugars. A tank of the fermentation unit can be equipped with at least one outlet, such that the fermentation broth can be removed via the at least one outlet.
A system described herein may comprise a xylitol refining unit, wherein the xylitol refining unit is configured to remove the xylitol from the fermentation broth. The xylitol refining unit can be in fluid communication with the fermentation unit. In some examples, the xylitol refining unit comprises one or more filters, such as microfilters, ultrafilters, and nanofilters. Optionally, the xylitol refining unit comprises three stages of filtration, such that the fermentation broth is subjected to microfiltration, ultrafiltration, and nanofiltration. The one or more filters may be in fluid communication with one or more columns, wherein the one or more columns may contain activated carbon, such as granulated active carbon, or an ion exchange resin, such as strongly acidic cation resin, weakly basic anion resin, or mixed bed resin. Optionally, the one or more columns are in fluid communication with an evaporation unit, wherein the evaporation unit is configured to evaporate water from the solution, thereby increasing the concentration of dissolved solids. Optionally, the xylitol refining unit comprises a xylitol crystallization unit. The xylitol crystallization unit can be in fluid communication with the evaporation unit. In some examples, the xylitol crystallization unit comprises a means for agitating the solution. Optionally, the xylitol crystallization is temperature controlled, such that the temperature of the unit can be gradually cooled. The xylitol crystallization unit may further comprise an inlet for receiving ethanol. In some examples, ethanol is added to the solution in the xylitol crystallization unit to assist xylitol crystallization. In some examples, the xylitol crystallization unit is configured to receive feed solution from the evaporation unit in batch or continuous mode. The xylitol crystallization unit may comprise a screen or filter to facilitate the separation of xylitol crystals from the mother liquor by filtration, or may be in fluid communication with a filter or centrifuge configured to receive the crystallization slurry. The separated xylitol crystals can be re-dissolved, and the resulting xylitol solution transferred to a xylitol polishing unit. In some examples, the xylitol polishing unit comprises an ion exchange resin, such as a SAC, WBA, or MB resin. Optionally, the xylitol polishing unit comprises active carbon, such as granulated active carbon.
In some examples, the described units are connected such that mass is transferred through sequential process steps. The solid feeding unit can transfer solid bagasse mass to a sizing mill either in batch or continuously. The sizing unit may be configured to transfer either in batch or continuously sized bagasse mass to the wash unit. This wash unit (1770) may be connected such that washed bagasse solid mass is transferred to the hemicellulose extraction unit either continuously or batch-wise. Optionally, the wash unit is also connected to a waste stream allowing removal of a solid waste stream comprising the removed soil and ash to a disposal location. The wash unit may optionally be connected to other process units further downstream to receive process water. The hemicellulose extraction unit (1700) may be connected to receive washed bagasse mass by solids transfer means. Optionally, the hemicellulose extraction unit is also connected at its output to the refining unit by means of liquid transfer. The hemicellulose extraction unit may also be connected to other processes that utilize the solid lignocellulose remainder stream by means of solid transfer. In some examples, the refining unit (1710) is connected by liquid transfer means to the hemicellulose extraction unit, feeding it extraction liquor. The refining unit can be connected by means of liquid transfer to a fermentation unit (1900), feeding it with the refined hemicellulose sugar stream as feed for xylitol fermentation. Alternatively, this refining unit is connected to a xylose fractionation unit (1720 and 1837) by means of liquid transfer. A schematic diagram of exemplary conversion processes to convert a xylose enriched hemicellulose sugar mixture (1720-P1) to downstream products is provided in
In some examples, the flux of mass transfer of the different connections is optimized to match fluxes upstream and downstream of each flux, so that units are optimized to be used efficiently. Energy can be transferred from unit to unit such that excess heat in one unit is utilized to heat another unit. Energy use throughout all the units disclosed herein may be optimized for the overall process.
In some examples, use of water is optimized for the overall process. Excess water produced in one unit can be transferred by liquid transfer means to be utilized where water is needed in another unit. Optionally, use of acid and base is optimized for the overall process to minimize need of fresh acid or base. For example, acidic streams resulting from regeneration of cation exchange resins by acid wash are used to regenerate Weak Acid Cation exchangers and/or acidify or neutralize streams in other units.
The system may be constructed such that it can feed at least 35,000 tons (dry solid) of sugar cane bagasse per year into the system, to produce at least 7,000 tons (dry solid) of refined hemicellulose sugars per year. The system is optionally constructed such that it can produce at least 5,000 tons (dry solid) xylose per year, at least 2,000 tons (dry solid) partially depleted xylose sugar mixture per year, along with at least 24,000 tons (dry solid) lignocellulose remainder. The system is optionally constructed such that it produces waste water at about 250 gpm.
It is understood that the examples and embodiments described herein are for illustrative purposes only and are not intended to limit the scope of the claimed invention. It is also understood that various modifications or changes in light the examples and embodiments described herein will be suggested to persons skilled in the art and are to be included within the spirit and purview of this application and scope of the appended claims. All publications, patents, and patent applications cited herein are hereby incorporated by reference in their entirety for all purposes.
The ash fraction of a sample of bagasse taken from a pile at a sugar mill in Louisiana was evaluated by ashing of samples in a microwave furnace (3.1. CEM Phoenix™ Microwave Muffle Furnace). The bagasse sample was found to contain 13.4% ash.
TABLE 1A
Ash results after different treatments to remove soil and ash
Sample
% Ash
Louisiana Sample R1
13.12
Louisiana Sample A
17.81
Louisiana Sample R2
13.38
Sample R1 washed with water
12.78
Sample A washed with water
17.16
Sample R2, 1 shear treatment, 1 pressure wash
6.67
Sample A, 2 shear treatments, 2 pressure wash
2.52
Sample R2, 6 shear treatments, 6 pressure wash
2.68
Sample R2, 8 shear treatments, 8 pressure wash
2.26
The results summarized in Table 1A demonstrate the high ash present in Louisiana bagasse obtained from different sugar mills and different sampling times. The results also show that to achieve effective removal of soil and ash it is essential to apply several cycles of shear treatment and washing with high pressure to cause the removal of stones, sand and sols of ash compound. The remaining bagasse still holds 2-3% of “true” ash, that is related to metal cations and other elements associated at molecular level in the cell structure.
Another sample of bagasse was milled and de-ashed, and the samples sieved through a series of screens before and after de-ashing.
TABLE 1B
De-soiling/De-ashing of bagasse
Ground Raw Bagasse
De-Ashed Bagasse
Screen
Screen
Fiber
Fiber
Size
Size (mm)
% ash
Length
% ash
Length
on 6 mesh
340
0.3
1.0-15.0
0
on 12
170
5
2.0-15.0
1
5.0-10.0
on 16
120
9.5
1.0-10.0
5.4
2.0-10.0
on 20
80
12.7
1.0-10.0
6
1.0-5.0
on 30
60
57.3
<1.0-5.0
71.1
1.0-5.0
thru 30
<60
15.4
<1.0
16.5
<1.0
The results summarized in Table 1B demonstrate the ability to remove by industrial means most of the soil and ash from bagasse feedstock by shear treatment and high pressure wash, while still maintaining ˜85% of the original feedstock at size greater than 30 mesh, that allows further handling of the washed material.
In practical operational conditions, an industrial process should be capable of utilizing bagasse of varying storage history, as bagasse may be stored in piles by the sugar mill for over 1, 3, 5, or even over 10, 12, or 14 years. Moreover, sugarcane harvesting season is about 3 months, with sugar production being a seasonal process, while a biorefinery should operate year round. It is further advantageous that excess leaves and field debris can be handled in the same process to harvest the xylose portion within and to eliminate a bottleneck of debris handling for the farmer and/or the sugar mill. Bagasse samples that have been stored more than a year, new bagasse and field debris were characterized. “New Bagasse” samples were from piles accumulated for up to 4 years ago, “Old Bagasse” samples were from piles accumulated 5-15 years ago, and “Leaves” and other field debris were de-soiled/de-ashed according to Example 1. The washed samples were heated to 160° C. for 60 minutes to extract hemicellulose sugars. Lignocellulosic biomass before and after extraction was analyzed according to NREL/TP-510-42622. Both solid phases and the hydrolysis liquor were analyzed for carbohydrate composition by HPAE-PAD. The results are summarized in Table 2. The results indicate that all samples can be handled by the methods and systems disclosed herein.
TABLE 2
Composition of different bagasse and field debris samples
New Bagasse
Old Bagasse
Leaves
Pre-
Post-
Pre-
Post-
Pre-
Post-
Hydrolysis
Hydrolysis
Hydrolysis
Hydrolysis
Hydrolysis
Hydrolysis
Dry Basis, % w/w
Solids
Solids
Solids
Solids
Solids
Solids
Hemicellulose
28.11
4.39
19.32
3.58
30.60
3.04
Cellulose
40.26
49.74
47.39
48.26
36.19
40.51
Klason lignin
20.52
27.08
26.45
31.21
19.07
30.76
Ash
2.1
6.49
2.27
10.08
3.56
3.89
TOTAL
91.36
88.24
95.93
96.24
89.97
78.95
Pre-
Post-
Pre-
Post-
Pre-
Post-
Individual Sugars
Hydrolysis
Hydrolysis
Hydrolysis
Hydrolysis
Hydrolysis
Hydrolysis
Dry Basis, % w/w
Solids
Solids
Solids
Solids
Solids
Solids
trehalose
0
0
0
0
0.00
0.00
arabinose
2.33
0.3
0.24
0.09
3.87
0.35
galactose
0.5
0.06
0.05
0.05
0.74
0.15
glucose
40.26
49.74
47.39
48.26
36.19
40.51
xylose
24.81
3.31
18.45
2.69
25.41
2.03
mannose
0.47
0.72
0.58
0.74
0.57
0.50
fructose
0.33
0.49
0.46
0.53
0.49
0.67
isomaltose
0
0
0
0
0.00
0.00
cellobiose
0
0
0
0
0.00
0.00
maltose
0
0
0
0
0.00
0.00
Aq conc; % w/w
Hydrolysate
Hydrolysate
Hydrolysate
trehalose
0
0
0.00
arabinose
0.08
0.005
0.12
galactose
0.02
0.005
0.02
glucose
0.12
0.088
0.25
xylose
0.58
0.326
0.59
mannose
0.03
0.006
0.01
fructose
0.02
0.003
0.03
isomaltose
0
0
0.00
cellobiose
0
0
0.00
maltose
0
0
0.00
xylose/monomers
68.2%
75.3%
57.1%
C6/xylose
32.8%
31.3%
54.7%
Bagasse was received from a sugar mill in lumps. The biomass was shredded using a wood chipper and screened through a series of sieves. Typical particle sizes of the crushed/shredded bagasse are presented in Table 3.
TABLE 3
Particle size of shredded bagasse
Mesh
Micron
% On
12
1680
6.2
20
841
3.6
30
595
16.5
40
420
20.4
60
250
21.6
80
177
10.2
100
149
5.9
120
125
2.4
200
74
6.5
Thru
74
7.3
100.6
Bagasse was shredded in a wood shredder. The shredded bagasse was washed in a temperature controlled tank and the washed bagasse (60 lbs, dry base) treated with an aqueous solution containing 0.5% H2SO4 (wt/wt) at a liquid to solid ratio of 14.2:1. The average temperature of the temperature controlled tank was maintained at 130-135° C. for 3 hours. The solution was circulated by pumping. The resulting liquor was collected, and the solids were washed with water. The wash water was then used to prepare the acid solution for the next batch by adding acids as needed. The hemicellulose-depleted lignocellulose remainder stream was collected and dried.
The acidic hemicellulose sugar stream was run through a SAC column. The sugar stream was then extracted continuously in a series of mixer settlers (2 stages) with an amine extractant (30:70 trilaurylamine:hexanol). The amine extractant to sugar stream ratio was kept in the range of 2:1 to 1.5:1. The resulting aqueous phase was further purified by using a SAC resin, a WBA resin, a granulated active carbon and a mixed bed resin. The pH of the resulting stream was adjusted to 4.5 with 0.5% HCl and the sugar solution was evaporated to a concentration of ˜30% DS. The resulting refined hemicellulose sugar stream contained about 7% arabinose, 2.5% galactose, 6.5% glucose, 65% xylose, 1.5% mannose, 4% fructose and 14% oligosaccharides (all % weight/total sugars). This sugar solution was further processed by fractionation on an SSMB system, resulting in a xylose rich fraction and a xylose depleted fraction. Each fraction was concentrated by evaporation. Table 4 provides a chemical analysis of the resulting xylose rich sugar solution.
TABLE 4
Chemical analysis of a xylose enriched sugar stream produced by
hemicellulose sugar extraction and purification from bagasse
PARAMETER
RESULT
UNITS
APPEARANCE
Colorless
pH
3.58
Saccharides
% TS (HPLC)
68.2
% w/w
Composition (HPAE-PAD)
XYLOSE
81.84 (55.81)
%/TS (%
ARABINOSE
4.38 (2.99)
%/TS (%
MANNOSE
1.99 (1.36)
%/TS (%
GLUCOSE
5.07 (3.46)
%/TS (%
GALACTOSE
0.91 (0.62)
%/TS (%
FRUCTOSE
6.15 (4.20)
%/TS (%
Impurities
Furfurals (GC)
<0.005
% w/w
Phenols (FC)
0.04
% w/w
Metals & inorganics (ICP)
Ca
<2
ppm
Cu
<2
ppm
Fe
<2
ppm
K
<2
ppm
Mg
<2
ppm
Mn
<2
ppm
Na
<2
ppm
S
<10
ppm
P
<10
ppm
Bagasse was shredded and de-soiled according to Examples 1 and 3 and the refined solids separated by filtration. The collected hemicellulose sugar stream was refined by first contacting with a SAC resin, followed by removal of much of the impurities by amine extraction. The refined aqueous sugar solution was further polished by contacting with a SAC resin, a WBA resin and finally evaporated to a concentration above 70% wt/wt dissolved sugars. The process was conducted at pilot scale at Virdia PDU, Danville, Va. Table 5 summarizes the sugar profile of the refined hemicellulose sugar streams.
TABLE 5
Sugar composition of a refined hemicellulose sugar stream produced
by hemicellulose sugar extraction and purification from bagasse
Sample
1
2
3
4
5
6
7
8
9
10
Average
Total Sugars (g)
87.53
87.53
86.68
89.79
76.02
87.81
76.25
71.41
81.11
88.41
83.25
Arabinose (g)
5.59
5.59
6.13
5.90
4.81
5.59
3.63
3.14
3.60
4.06
4.80
Galactose (g)
2.05
2.05
2.12
2.03
1.62
2.02
1.84
1.74
1.78
1.95
1.92
Glucose (g)
5.09
5.09
5.58
5.33
4.65
6.79
7.15
6.75
7.54
6.79
6.07
Xylose (g)
58.69
58.69
56.58
59.05
52.14
58.11
50.65
47.21
56.24
55.10
55.25
Mannose (g)
1.51
1.51
1.12
1.43
1.30
2.27
2.22
2.09
2.27
1.84
1.75
Fructose (g)
3.12
3.12
3.37
1.97
1.54
2.52
2.86
2.94
2.16
3.49
2.71
As evidenced in Table 5, a refined hemicellulose sugar stream produced from bagasse comprises, on average, 66% xylose, 6% arabinose, and 15% hexoses, all weight/weight relative to total sugars. The streams exemplified in Table 5 are thus suitable for use in the subject methods for conversion to xylitol.
Refined hemicellulose sugar streams 1 to 10 produced according to Example 5 were fractionated by chromatography (as per PCT/US2013/039585) to produce xylose enriched extract streams 1 to 10 (Table 6A) and xylose depleted raffinate streams 1 to 10 (Table 6B). A pulse test chromatogram showing fractionation of a refined hemicellulose sugar stream is provided in
TABLE 6A
Sugar composition of a xylose enriched sugar mixture produced from bagasse
Sample
1
2
3
4
5
6
7
8
9
10
Average
Total Sugars (g)
45.01
45.01
67.60
66.06
70.42
69.72
44.97
63.04
58.11
46.74
57.67
Arabinose (g)
0.23
0.23
3.35
4.38
3.60
3.91
1.06
2.16
1.60
0.96
2.15
Galactose (g)
0.04
0.04
0.58
0.96
0.69
0.73
0.25
0.76
0.48
0.20
0.47
Glucose (g)
0.37
0.37
3.31
4.52
3.57
4.16
1.85
4.08
3.20
1.36
2.68
Xylose (g)
39.09
39.09
57.86
53.33
60.13
55.34
38.27
51.98
50.18
39.89
48.51
Mannose (g)
0.23
0.23
0.69
1.32
0.84
1.91
0.80
1.64
1.40
0.88
1.00
Fructose (g)
0.68
0.68
1.78
1.55
1.58
3.67
2.75
2.40
1.20
3.40
1.97
TABLE 6B
Sugar composition of a xylose depleted sugar mixture produced from bagasse
Sample
1
2
3
4
5
6
7
8
9
10
Average
Total Sugars (g)
18.00
18.00
19.15
18.00
10.24
17.62
15.32
12.68
19.53
22.98
17.15
Arabinose (g)
2.32
2.32
2.42
1.63
1.14
1.84
1.21
1.24
2.07
2.11
1.83
Galactose (g)
1.36
1.36
1.32
1.00
0.63
1.12
1.07
0.94
1.53
1.49
1.18
Glucose (g)
1.88
1.88
2.02
1.27
0.89
1.53
2.54
2.64
4.79
3.75
2.32
Xylose (g)
2.87
2.87
3.17
3.82
2.14
3.78
3.13
2.51
4.60
5.02
3.39
Mannose (g)
0.36
0.36
0.42
0.28
0.15
0.29
0.45
0.46
0.84
0.80
0.44
Fructose (g)
0.57
0.57
0.65
0.51
0.20
0.19
0.72
0.46
0.57
1.07
0.55
As evidenced in Table 6A, a xylose enriched sugar mixture produced from bagasse comprises, on average, 84% xylose, 4% arabinose, and 11% hexoses, all weight/weight relative to total sugars. Some xylose enriched mixtures, such as Sample 3, have a lower concentration of hexoses (86% xylose, 5% arabinose, and 9% hexoses). On average, the samples exemplified in Table 6A are suitable for use in the subject methods for conversion to xylitol, although some of the individual samples may contain a higher than ideal ratio of xylose to hexoses. Surprisingly, fractionation of a refined hemicellulose sugar stream may not be necessary to produce a sugar stream suitable for conversion to xylitol.
As evidenced in Table 6B, a xylose depleted sugar mixture produced from bagasse comprises, on average, 20% xylose, 11% arabinose, and 26% hexoses, all weight/weight relative to total sugars.
The refined hemicellulose sugar streams disclosed herein are particularly suitable as feed for fermenting species capable of hydrogenating xylose to xylitol with high specificity, and capable of using the C6 sugars as well as at least some of the arabinose as their energy source for proliferation. Table 7 summarizes typical refined hemicellulose sugar streams suitable to be fed for xylitol production.
TABLE 7
Sugar composition of a refined hemicellulose sugar stream suitable as feed for xylitol fermentation
Sample
AC130418
AC130419
AC130420
AC130422
AC130423
AC130424
AC130502
AC130507
AC130508
AC130517
Average
Xylose
77.2
77.2
75.5
78.0
78.9
75.2
74.1
73.9
76.4
75.3
76.1
(%/monomers)
Arabinose
7.4
7.4
8.2
7.8
7.3
7.2
5.3
4.9
4.9
5.5
6.6
(%/monomers)
C6 sugars
15.5
15.5
16.3
14.2
13.8
17.6
20.6
21.2
18.7
19.2
17.3
(%/monomers)
The ability to purify xylitol from a mixture containing xylitol, arabitol, and xylose by crystallization and chromatography was evaluated. Crystallization was performed in an agitated, jacketed beaker attached to a circulating water heater/cooler. A solution was made to simulate a fermentation product: 300 g of a solution containing 93.9% xylitol, 3.7% xylose, and 2.8% arabitol/arabinose was diluted to 79.2% DS, and ethanol added according to the total weight of solvent at indicated mol %. Crystallization was initiated at 65° C. by seeding with xylitol and the solution cooled to 35° C. over 16 h. Crystals were collected by filtration, washed with ethanol, dried, and analyzed for xylitol purity by HPAE-PAD. Xylitol yield and purity are summarized in Table 8. It is observed that high yield of xylitol was achieved (e.g. 77% in one crystallization), with the xylitol being 99.9% pure of reducing sugars and arabitol.
TABLE 8
Yield and purity of xylitol crystals
%
Xylitol
Xylitol
Residual
Residual
Ethanol
yield, %
purity, %
arabitol, ppm
xylose, ppm
10
77
99.9
200
570
Xylitol was fractionated from a mixture containing 43% weight/weight xylitol, 6% weight/weight arabitol, 6% weight/weight xylose, and 8% weight/weight ethanol. The composition of this mixture is representative of major components present in the crystallization mother liquor.
A pulse test was conducted utilizing 250 mL of Purolite PCR 642 (gel form, styrene divinylbenzene copolymer, functional group sulfonic acid, and mean bead size 295-335 μm). The gel was pre-conditioned with a solution containing strontium salt to make it fully in a strontium form. A 12.5 mL sample of the xylitol mixture was injected, followed by water elution at 8.33 mL/min. Effective fractionation of xylitol from the mixture was observed, with the xylose peaking at 0.61 BV, ethanol at 0.72 BV, arabitol at 0.84 BV and xylitol peaking at 0.96 BV. The pulse test results are described in
A system as described schematically in
Washed bagasse was heated to extract the hemicellulose sugars in batches of 2000-3000 Lb under conditions similar to Example 4. The collected slurry was continuously fed into a 0.6 m2 Stainless Steel 024 Filter (BHS Sonthofen Inc). The slurry, having a solids concentration of 7.5-8%, was fed at 70° C. at a throughput of 0.5-1.5 gal/min (average approximately 1 gal/min). The wash liquid was city water at 70° C. Polypropylene (850 μm thick, air permeability of 50 L/m2S) was used as a filtration material. Prior to filtration, the slurry was sparged with steam to increase the temperature to 70° C. The slurry was agitated and heated in the totes using the steam and an air dispersion device. The slurry was then pumped to the filter using a diaphragm pump. The filter cake was washed with hot water. The filter cake was allowed to dewater under vacuum and discharged via a 90 degree roller. The cake was analyzed for moisture, ash and for residual free sugars, with results summarized in Table 11, showing effective washing and de-watering of the lignocellulose remainder stream. The clarity of filtrate was evaluated by centrifuging a sample of the filtrate. The solid content of the mother filter was estimated as less than 0.1%, and no solid content was visualized in the wash filtrate, indicating that the solids were efficiently removed by filtration.
TABLE 11
Moisture, ash and residual sugar in
the lignocellulose remainder stream
Residual
Reference No.
sugars (% wt/wt)
Moisture (% wt/wt)
Ash (% wt/wt)
21888
0.4
73.4
5.5
21892
1.9
74.9
2.8
21896
0.7
72.9
3.0
21787
1.0
73.0
3.6
21752
0.7
72.5
3.0
21791
1.1
71.8
5.4
21795
0.3
72.2
4.8
21853
0.5
72.7
3.0
21884
NA
74.8
NA
Average
0.8
73.1
3.9
STDV
0.5
1.1
1.2
The hemicellulose hydrolysate collected in Example 11 was refined by contacting with a SAC resin followed by amine extraction. The refined aqueous solution was evaporated to strip off the solvent, then further polished by contacting with a SAC resin, a WBA resin, a MB resin, and finally evaporation to about 70% wt/wt DS. The final sugar products were analyzed and shown to have the compositions of Table 12A. Some of the material was fractionated by chromatography to enrich the xylose fraction, the composition of which is provided in Table 12B. Both samples were successfully fermented to xylitol by various microorganisms, with appropriate addition of C6 sugars (e.g., glucose) to support the proliferation of the microorganism.
TABLE 12A
Sugar composition of a refined hemicellulose sugar stream produced
by hemicellulose sugar extraction and purification from bagasse
PARAMETER
RESULT
UNITS
APPEARANCE
Colorless, clear
solution
pH
4.08
Saccharides
DS (HPLC)
68.64
% wt/wt
Degree of Polymerization
(HPLC)
Monomers
98.80
%
Oligomers
1.20
%
Composition (HPAE-PAD)
XYLOSE
57.58
% of monomers
ARABINOSE
8.09
% of monomers
MANNOSE
2.61
% of monomers
GLUCOSE
16.84
% of monomers
GALACTOSE
2.21
% of monomers
FRUCTOSE
12.67
% of monomers
Impurities
Furfurals (UV)
<0.01
% wt/wt
Phenols (UV)
0.02
ppm/DS
Metals & inorganics (ICP)
Ca
11
ppm/DS
Cu
<2
ppm/DS
Fe
<2
ppm/DS
K
<2
ppm/DS
Mg
2
ppm/DS
Mn
<2
ppm/DS
Na
110
ppm/DS
S
<16
ppm/DS
P
<23
ppm/DS
Reference: DB4D01
TABLE 12B
Sugar composition of a xylose-enriched sugar stream produced by
hemicellulose sugar extraction and purification from bagasse
PARAMETER
RESULT
UNITS
APPEARANCE
Colorless viscous
liquid, crystal slurry
Saccharides
DS (HPLC)
78.80
% wt/wt
Degree of polymerization
(HPLC)
Monomers
98.11
%
Oligomers
1.89
%
Composition (HPAE-PAD)
XYLOSE
83.71
% of monomers
ARABINOSE
2.97
% of monomers
MANNOSE
2.01
% of monomers
GLUCOSE
5.39
% of monomers
GALACTOSE
0.83
% of monomers
FRUCTOSE
5.09
% of monomers
Impurities
Furfurals (UV)
<0.005
% wt/wt
Phenols (UV)
0.04
ppm/DS
Metals & inorganics (ICP)
Ca
<2
ppm/DS
Cu
<2
ppm/DS
Fe
<2
ppm/DS
K
<2
ppm/DS
Mg
<2
ppm/DS
Mn
<2
ppm/DS
Na
<2
ppm/DS
S
<10
ppm/DS
P
<10
ppm/DS
Reference: DB4D02
Bagasse from Raceland, La. was de-ashed according to Example 10 and extracted and separated as described in Example 11. Samples of the solid biomass were collected after each process step, dried and analyzed for their composition. Table 13 summarizes the results, indicating efficient de-ashing of the solid in the de-ashing/de-soiling step, and efficient extraction of hemicellulose sugars as well as reducing much of the remaining metal elements present in biomass by extracting the physiologically bound metals at the extraction step. The de-ashed biomass is anticipated to be much more suitable than the feed biomass for usage as feed for energy uses, e.g. oxidative burning to produce energy directly or pyrolysis to produce bio-oil. The hemi-depleted biomass is anticipated to be an even better feed for energy purposes, as more inorganic content is removed as well as some carbohydrates, consequently the percentage of lignin is increased from an average of ˜24% to an average of ˜40%. The higher lignin content and lower sugar content results in higher energy density of the biomass.
TABLE 13
Raceland bagasse composition analysis after the de-ashing step and after hemicellulose extraction step
Compositional Analysis - % dry basis
Moisture
Total
Carbohydrate Composition
Sample Name
(% w/w)
Ash
Lignin
carbohydrate
Glucose
Xylose
Arabinose
Galactose
Mannose
De-ashed 1
54.6
4.7
23.81
66.98
42.58
21.41
1.00
0.25
1.24
De-ashed 2
58.5
4.8
24.03
66.16
40.62
22.62
0.97
0.24
1.22
De-ashed 3
57.7
3.9
23.28
68.35
40.48
24.53
1.19
0.24
1.43
De-ashed 4
55.2
3.6
23.45
67.41
39.95
24.02
1.23
0.25
1.47
De-ashed 5
53.2
3.1
23.36
70.31
41.71
25.26
1.19
0.48
1.19
Hemi-depleted 1
64.1
4.2
39.32
57.76
52.42
4.37
0
0
0.73
Hemi-depleted 2
71.7
5.4
39.65
61.9
57.60
4.30
0
0
0
Hemi-depleted 3
66.9
4.1
31.85
57.05
54.62
2.43
0
0
0
Hemi-depleted 4
66.4
5.1
47.47
47.19
45.19
2.00
0
0
0
Hemi-depleted 5
68.2
5
42.89
52.8
49.61
3.19
0
0
0
Compositional Analysis - % dry basis
Carbohydrate Composition
ICP Results - ppm dry basis
Sample Name
Fructose
S
Ca
Fe
K
Mg
Na
De-ashed 1
0.5
81
1800
1600
590
560
120
De-ashed 2
0.49
67
980
1200
580
510
120
De-ashed 3
0.48
61
710
970
400
360
65
De-ashed 4
0.49
44
690
970
340
350
50
De-ashed 5
0.48
44
800
830
240
320
120
Hemi-depleted 1
0.24
780
120
130
88
63
500
Hemi-depleted 2
0
730
97
130
88
56
490
Hemi-depleted 3
0
2300
190
240
92
84
620
Hemi-depleted 4
0
1900
150
180
82
67
650
Hemi-depleted 5
0
3700
330
380
170
140
460
A fermenter containing fermentation media (tryptone, 14 g; yeast extract, 7 g; potassium phosphate, dibasic, 4.2 g; sodium chloride, 7 g; magnesium sulfate, 2 g; water, 750 mL, antifoam Cognis Clerol FBA 3107, 3 drops) is sterilized as described in U.S. Pub. No. 2013/0217070. A refined hemicellulose sugar stream prepared according to the subject methods (e.g., as in Examples 5 and 7) is added (100 mL, comprising 30 g of xylose). The fermenter is inoculated with 50 mL of a starter culture of a suitable microorganism (e.g., ZUC220 or ZUC170) at 30° C., and the fermentation allowed to run at 30° C. and pH 7.0 (NH4OH controlled) with agitation (800 RPM) and introduction of air at 1 LPM as described in U.S. Pub. No. 2013/0217070. The volume after inoculation is 900 mL. After 24 hours, additional refined hemicellulose sugar stream is added (185 mL, comprising 130 g of xylose). The fermentation is allowed to run for a total of 80 hours after inoculation before separating the microorganism from the xylitol stream by filtration. Xylitol is crystallized as described in Example 8. Fermentation methods of the disclosure may display a volumetric productivity of greater than 1.5 g/L/h (“A” productivity), from 1.0 to 1.5 g/L/h (“B” productivity), from 0.5 to 1.0 g/L/h (“C” productivity), or less than 0.5 g/L/h (“D” productivity). In some examples, the xylitol yield of the fermentation methods described herein is greater than 100 g/L (“A” yield), from 75 to 100 g/L (“B” yield), from 50 to 75 g/L (“C” yield), or less than 50 g/L (“D” yield). Further examples of fermentation conditions can be found, for example, in U.S. Pub. No. 2013/0217070.
Protein and amino acids are usually present in biomass feedstock and can be removed from sugar solutions to avoid inhibition of some microorganisms used for industrial fermentation processes. This may be necessary when sugar cane leaves are used as feedstock, as inherently more protein and amino acids are present in leaves than in the cane. Samples of bagasse and leaves were hydrolyzed and refined as described in Example 5. Samples of bagasse, leaves, and refined hemicellulose sugar streams derived from the same were analyzed by Galbraith Laboratories, Inc. for nitrogen and protein content, with the results summarized in Table 15. It can be seen that nitrogen containing molecules have been removed efficiently in the refining process, as both samples comprise less than 200 ppm nitrogen.
TABLE 15
Nitrogen and protein analysis in biomass and refined
hemicellulose sugar streams produced from same
Nitrogen
Protein (Wet
Sample
(Kjeldahl)
Chemistry)
Bagasse
1121
ppm
7005 ppm
Sugarcane leaves
5574
ppm
34800 ppm
Refined hemicellulose sugar
13
ppm
Not Determined
stream from bagasse, ca. 65% DS
Refined hemicellulose sugar
147
ppm
Not Determined
stream from leaves, ca. 65% DS
1. A method of producing xylitol from a lignocellulose-containing biomass, comprising:
Jansen, Robert, Lapidot, Noa, Lawson, James Alan, Travisano, Philip, Carden, Adam Tyler, Stout, Brendon Christopher
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